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REPORT 


ON    THE    INVESTIGATIONS    INTO 


THE  PURIFICATION  OF  THE  OHIO  RIVER 
WATER  AT  LOUISVILLE  KENTUCKY 


MADE    TO   THE 


PRESIDENT  AND  DIRECTORS 


OF   THE 


LOUISVILLE   WATER  COMPANY 


BY 

GEORGE  W.  FULLER 


PUBLISHED    UNDER   AGREEMENT    WITH    THE  DIRECTORS 


NEW   YORK 

D.  VAN  NOSTRANL)  COMPANY 
1898 


TABLE  OF  CONTENTS. 


INTRODUCTION T 

Location,  scope,  and  principal  dates  of 
the  investigations.  Nature  of  systems  of 
purification  tested.  Character  of  the  War 
ren,  Jewell,  and  Western  systems.  The 
Harris  device.  The  Mark-Brownell  de 
vices.  The  MacDougall  polarite  system. 
Methods  and  devices  of  the  Water  Company. 
The  development  of  water  purification  ;  its 
state  at  the  beginning  of  these  tests  and  an 
historical  resume.  Most  important  types  of 
filters  abroad.  Principles  of  sand  filtration 
without  coagulants.  English  filters.  Modi 
fication  of  English  filters.  English  filters  in 
America.  American  filters.  Efficiency  of 
American  filters  and  their  cost.  Conditions 
under  which  the  tests  were  conducted.  List 
of  chapters. 

CHAPTER    I. 
COMPOSITION  OF  THE  OHIO  RIVER  WATER..      15 

Character  of  watershed.  Freshets  in 
the  Ohio  River,  with  annual  comparisons, 
1861-96.  Plan  of  analytical  work.  Physi 
cal  character  of  Ohio  River  water.  Chemical 
character  of  Ohio  River  water,  with  tables 
of  daily  analyses.  Special  chemical  anal 
yses.  Biological  character  of  Ohio  River 
water.  Results  of  microscopical  analyses. 
Species  of  bacteria  found.  Number  of  bac 
teria  in  Ohio  River  water  by  days. 

CHAPTER    II. 

DESCRIPTION  OF  THE  APPLICATION  OF  CHEM 
ICALS  TO  THE  OHIO  RIVER  WATER  BY  THE 
SEVERAL  SYSTEMS  OF  PURIFICATION 40 

Kinds  of  chemicals  used.  Composition 
of  chemicals  used.  Devices  used  by  the  re 
spective  systems  for  the  application  of 


chemicals.  Uniformity  in  rate  of  applica 
tion  of  the  chemicals.  Strengths  of  chemi 
cal  solutions,  their  uniformity,  and  daily 
averages  for  the  respective  systems.  Aver 
age  daily  amounts  of  sulphate  of  alumina 
used  by  the  respective  systems.  Average 
daily  amounts  of  lime  used  by  the  Jewell 
system. 

CHAPTER    III. 

DECOMPOSITION  AND  SUBSEQUENT  DISPOSAL 
OF  THE  ALUM  OR  SULPHATE  OF  ALUMINA 
APPLIED  TO  THE  OHIO  RIVER  WATER....  53 

The  general  action  of  the  chemical  upon 
its  addition  to  the  water.  Reduction  of 
alkalinity  by  the  applied  chemical.  Ab 
sorption  of  applied  chemical  by  suspended 
matters.  Methods  of  daily  tests  for  excess 
of  chemical.  Presence  of  traces  of  unde- 
composed  chemical  in  filtered  water  at  rare 
intervals.  Undecomposed  chemical  in  efflu 
ent  in  practice  inadmissible  and  inexcu 
sable. 

CHAPTER    IV. 

COAGULATION  AND  SEDIMENTATION  OF  OHIO 
RIVF.R  WATER  BY  ALUMINUM  HYDRATE 
FORMED  BY  THE  DECOMPOSITION  OF  THE 
APPLIED  ALUM  OR  SULPHATE  OF  ALU 
MINA 57 

General  action  of  a  coagulant.  Coagula 
tion.  Sedimentation.  Devices  for  coagu 
lation  and  sedimentation  in  the  respective 
systems.  Purification  by  sedimentation  in 
the  several  systems.  Bacteria  in  the  efflu 
ent  of  the  Warren  and  Jewell  settling-cham 
bers.  Special  sedimentation  experiments. 
Bacteria  in  the  Louisville  water  supply  as 
drawn  from  city  taps,  with  the  average  puri 
fication  effected  by  the  distributing  system. 


TABLE   OF   CONTENTS. 


CHAPTER    V. 

DESCRIPTION  OF  THE  FILTERS  THROUGH 
WHICH  THE  RIVER  WATER  PASSED  AFTER 
COAGULATION  BY  ALUMINUM  HYDRATE 
AND  PARTIAL  PURIFICATION  BY  SEDIMEN 
TATION 70 

General  account  of  the  leading  features 
of  all  the  filters.  The  Warren  filter.  The 
Jewell  filter.  The  Western  gravity  filter. 
The  Western  pressure  filter. 

CHAPTER    VI. 

SUMMARY  OF  THE  VARIOUS  PARTS  OF  THE 
RESPECTIVE  SYSTEMS,  AND  A  RECORD  OF 
REPAIRS,  CHANGES,  AND  DELAYS 89 

List  of  the  principal  parts  of  the  purifica 
tion  station.  Schedules  of  the  devices  and 
appurtenances  employed  for  application  of 
chemicals,  ^sedimentation  and  coagulation, 
and  filtration,  respectively,  in  each  system. 
Repairs  and  changes  of  the  respective  sys 
tems.  Delays  in  operation  during  the  tests. 
Summary  of  the  time  occupied  in  various 
ways  during  the  tests. 

CHAPTER    VII. 

THE  MANNER  OF  OPERATION  OF  THE  RE 
SPECTIVE  SYSTEMS  OF  PURIFICATION,  AND 
THE  AMOUNT  OF  ATTENTION  GIVEN 
THERETO .  96 

General  manner  of  operation.  Detailed 
method  of  operation  of  each  of  the  systems. 
Mechanical  devices  used  to  aid  in  the 
operation  of  the  respective  systems.  Atten 
tion  given  to  the  respective  systems. 

CHAPTER  VIII. 

COMPOSITION  OF  THE  OHIO  RIVEK  WATER 
AFTER  TREATMENT  BY  THE  RESPECTIVE 
S\ STEMS  OF  PURIFICATION,  AS  SHOWN  BY 
CHEMICAL,  MICROSCOPICAL,  AND  BACTERIAL 
ANALYSES  ;  TOGETHER  WITH  A  TABULATION 
OF  THE  MOST  IMPORTANT  DATA  ON  THE 
OPERATION  OF  THE  RESPECTIVE  SYSTEMS..  .  108 

Description  of  tables.  Results  of  chem 
ical  analyses  of  effluents  of  the  respective 
systems.  Results  of  mineral  analyses  of 
effluents.  Results  of  bacterial  analyses  of 
effluents.  Records  of  operation  of  the  re 
spective  systems  by  runs,  with  summaries  of 
the  leading  analytical  results  for  each  run. 


CHAPTER  IX. 

SUMMARY  OF  THE  PRINCIPAL  DATA  UPON  THE 
EFFICIENCY  AND  ELEMENTS  OF  COST  OE 
PURIFICATION  BY  THE  RESPECTIVE  SYS 
TEMS,  OF  THE  OHIO  RIVER  WATER,  DIVIDED 
INTO  TWENTY  PERIODS,  ACCORDING  TO  THE 
CHARACTER  OF  THE  UNPURIFIED  WATER  ; 
TOGETHER  WITH  A  DISCUSSION  OF  SOME  OF 
THE  MORE  IMPORTANT  FEATURES 215 

Description  of  summaries.  Periods  into 
which  the  investigations  are  divided.  Daily 
appearance  of  the  effluents.  Daily  amounts 
ot  organic  matter  in  the  river  water  and  the 
percentage  removal  by  the  respective  sys 
tems.  Daily  number  of  bacteria  in  the  river 
water  and  effluent  of  each  of  the  respective 
systems,  together  with  their  bacterial  effici 
ency.  Summaries  of  the  leading  results  for 
each  of  the  twenty  periods.  Total  quantities 
for  the  entire  investigation  of  1895-96  and 
leading  averages.  Final  summaries  of  re 
sults. 

Outline  of  methods  followed  in  the  discus 
sion.  Quality  of  Ohio  River  water  after 
purification,  with  reference  to  the  efficiency 
of  the  respective  systems,  and  the  general 
effect  of  this  method  of  purification  on  the 
character  of  the  effluent. 

Prominent  factors  which  influenced  the 
quality  of  the  effluent  and  cost  of  purifica 
tion,  among  which  were  the  following  :  Com 
position  of  the  river  water  ;  application  of 
alum  or  sulphate  of  alumina  ;  quantity  of  ap 
plied  alum  or  sulphate  of  alumina;  provisions 
for  the  removal  of  suspended  matter  from 
the  river  water  by  sedimentation  ;  degree  of 
coagulation  of  the  partially  subsided  water 
as  it  entered  the  sand  layer  ;  sand  layers  of 
the  several  filters  ;  rate  of  filtration  ;  regula 
tion  and  control  of  operation  of  the  filters  ; 
loss  of  head  ;  washing  the  sand  layer  ;  and 
the  effect  of  proper  attention. 

Comparison  of  the  elements  of  cost  of 
purification  of  25  million  gallons  of  the  Ohio 
River  water  daily  by  the  respective  systems, 
based  on  the  results  of  ten  months'  tests  of 
25o,ooo-gallon  systems. 

General  conclusions  in  regard  to  the  tests 
of  1895-96.  Applicability  of  the  American 
method  to  the  clarification  and  purification 
of  Ohio  River  water.  General  defect  of  all 
systems  in  the  lack  of  proper  provisions  for 
subsidence  and  its  effect  on  the  application 


TABLE   OF   CONTENTS. 


of  this  method  of  purification  to  the  Ohio 
River  water.  Comparison  of  the  principal 
devices  of  the  respective  systems.  Quality 
of  the  filtered  Ohio  River  water.  Final  con 
clusions  on  the  1895-96  data. 

CHAPTER  X. 

DESCRIPTION  OF  THK  HARRIS  MAGNETO- 
ELECTRIC  SYSTEM  OF  PURIFICATION,  AND 
A  RECORD  OF  THE  RESULTS  ACCOMPLISHED 
THEREWITH 276 

General  description.  Spark  drum.  Elec 
trolytic  tanks.  Magnets.  Electrodes.  Re 
sults  accomplished  by  the  system. 

CHAPTER  XI. 

DESCRIPTION  OF  THE  DEVICES  OPERATED  BY 
THE  HARRIS  COMPANY  IN  JULY,  1896,  AND 
A  RECORD  OF  THE  RESULTS  ACCOMPLISHED 
THEREWITH  280 

First  Experiments.  Situation  on  July  i, 
1896.  Description  of  devices  Nos.  i,  2,  3, 
4,  and  5,  and  records  of  the  results  accom 
plished  therewith,  respectively.  Summary 
of  results  accomplished  with  device  No.  5. 
Status  of  the  situation  on  Aug.  i,  1896. 

CHAPTER  XII. 

INVESTIGATIONS  BY  THE  WATER  COMPANY  IN 
AUGUST  INTO  THE  PRACTICABILITY  AND 
ECONOMY  OF  THE  DEVICES  OPERATED  BY 
THE  HARRIS  COMPANY 292 

The  direct  and  indirect  effect  of  the 
application  of  electricity  upon  the  bacteria 
and  organic  matter  in  the  river  water,  and  in 
the  purification  of  the  water  through  the 
formation  of  aluminum  hydrate  from  alu 
minum  electrodes.  Comparison  of  the 
coagulating  power  of  aluminum  hydrate 
formed  electrolytically  and  from  sulphate  of 
alumina,  respectively.  Action  of  electro 
magnets.  Rate  and  regularity  of  electrolytic 
formation  of  aluminum  hydrate.  Amount 
of  metallic  aluminum  wasted  in  this  electro 
lytic  process.  Relative  cost  of  aluminum 
hydrate  formed  electrolytically  and  from 
chemicals.  On  the  amount  of  power  re 
quired  on  a  large  scale  to  produce  aluminum 
hydrate  by  means  of  electricity. 


CHAPTER  XIII. 

DESCRIPTION  OF  THE  MARK  AND  BROWNELI. 
ELECTROLYTIC  DEVICES,  AND  A  RECORD  OF 
THE  RESULTS  ACCOMPLISHED  THEREWITH  301 

An  account  of  preliminary  experiments 
made  in  the  laboratory  of  the  Louisville 
Manual  Training  School.  Description  of  elec 
trolytic  appliances  used  in  connection  with 
the  Jewell  filter  and  of  the  conditions  under 
which  the  tests  were  conducted.  Electric 
generating  plant.  Electrolytic  cells.  Iron 
electrodes.  Outline  of  the  operation  of  these 
devices.  Summary  and  discussion  of  results 
obtained.  Deposition  of  iron  hydrate  at  the 
bottom  of  the  cells  and  its  subsequent  loss. 
Irregularities  of  the  flow  of  water  through 
the  cells.  Variations  in  the  conductivity  of 
the  river  water.  Electric  power  used  by 
these  devices.  General  status  of  this  proc 
ess  at  the  close  of  these  tests.  Brownell 
electrodes.  Mark  electrodes.  Brief  com 
parison  of  the  relative  efficiency  of  iron 
and  aluminum  electrodes.  Records  of  oper 
ation  and  results  of  analyses. 

CHAPTER  XIV. 

DESCRIPTION  OF  THE  MACDOUGALL  POLARITE 
SYSTEM,  AND  A  RECORD  OF  THE  RESULTS 
ACCOMPLISHED  THEREWITH 318 

Preliminary  plans.  General  description. 
Detailed  description  of  iron  tank  with  baffle- 
plates,  and  of  the  clay  extractor.  Descrip 
tion  of  the  polarite  filter,  and  modifications 
of  the  same.  Character  of  the  filtering  mate 
rials.  Composition  of  polarite  used.  Opera 
tion  of  the  system,  general  description  and 
detailed  records.  Special  method  of  clean 
ing  the  Jewell  filter.  Quality  of  the  Ohio 
River  water  after  treatment  by  this  system. 
Results  of  analyses  in  detail.  Applicability 
of  this  method  for  the  purification  of  the 
Ohio  River  water. 

CHAPTER  XV. 

DESCRIPTION  OF  THE  METHODS  AND  DEVICES 
OF  THE  WATER  COMPANY,  TESTED  DURING 
1897,  AND  A  RECORD  AND  DISCUSSION  OF 
THE  RESULTS  ACCOMPLISHED  THEREWITH  . .  333 

Status  of  the  problem  on  March  10,  1897. 
Objects  of  the  investigations  of  1897.  Plan 
of  presentation  of  the  results.  General  de- 


TABLE   OF   CONTENTS. 


scription  of  the  devices  employed.  Detailed 
description  of  the  settling  basins;  devices 
for  the  application  of  chemical  solutions; 
solutions  used  ;  and  devices  for  the  applica 
tion  of  electrolytic  treatment.  The  arrange 
ments  for  use  of  the  Jewell  filter.  General 
adaptability  of  devices  employed,  with  their 
limitations.  Description  of  the  methods  and 
conditions  of  operation  of  these  devices. 
General  notes  on  the  records  of  operation. 
Results  accomplished  by  these  devices. 
Tables  of  analyses.  Summary  of  the  results 
of  analyses  showing  the  amount  of  suspended 
matter  and  number  of  bacteria  in  the  river 
water  as  it  passed  through  the  several  set 
tling  basins.  Final  summary  of  the  leading 
results  of  the  operation  of  the  devices. 

Discussion  of  the  results,  arranged  for  con 
venience  tinder  fifteen  sections. 

Section  No.  i. — Purification  of  the  Ohio 
River  water  by  plain  sedimentation.  Limited 
evidence  available.  Probable  effect  of  24 
and  48  hours'  plain  subsidence.  Efficiency 
of  basins  used.  Effect  of  character  of  sus 
pended  matter  on  removal  by  plain  subsid 
ence.  Effect  of  conditions  of  plain  subsid 
ence  on  percentage  removal.  General  con 
clusions. 

Section  No.  2. — Account  of  the  commer 
cial  chemicals  available  as  coagulants  for 
the  Ohio  River  water,  and  of  their  behavior 
when  applied  to  the  water.  Classification  of 
metals  in  their  applicability  to  the  purifica 
tion  of  Ohio  River  water.  Most  suitable 
compounds  capable  of  producing  coagulat 
ing  precipitates,  and  a  description  of  their 
behavior. 

Section  No.  3. — General  description  of 
electrolysis.  Special  methods  and  devices 
for  electrolysis  arranged  by  the  Water  Com 
pany.  Fundamental  laws  and  principles  of 
electrolysis  as  applied  to  the  electrolytic 
formation  of  hydrates  of  iron  and  aluminum 
in  the  Ohio  River  water. 

Section  No.  4. — Detailed  account  of  the 
electrolytic  formation  of  iron  hydrate  in 
Ohio  River  water.  Passivity  of  iron  elec 
trodes  to  the  ions  of  Ohio  River  water. 
Cause  of  passivity— initial  and  acquired. 
Form  in  which  the  iron  leaves  the  electrodes. 
Influence  on  the  process  of  oxygen,  free  car 
bonic  acid,  hydrogen,  and  solubility  of  the 
initial  iron  compounds.  Form  in  which  the 


iron  leaves  the  electrolytic,  cell.  Natural 
limitations  of  the  electrolytic  treatment 
with  iron  electrodes.  Rate  of  decomposi 
tion  of  iron  at  the  positive  electrodes. 
Rate  of  deposition  of  iron  on  the  nega 
tive  electrodes.  Rate  and  uniformity  of 
formation  of  available  hydrate.  Influ 
ence  on  the  formation  of  hydrate — of  the 
potential  difference  between  the  plates,  of 
the  current  density,  of  the  composition  of 
the  iron,  of  the  composition  of  the  river 
water,  of  reversing  the  direction  of  the  elec 
tric  current,  and  of  allowing  the  electrodes 
to  remain  out  of  service.  Metal  wasted  in 
the  process.  Electric  resistance  of  films  of 
iron  oxide.  Power  wasted  in  the  process. 
Effect  of  this  process  on  subsidence,  filtra 
tion,  and  composition  of  the  filtered  water. 
Conclusions. 

Section  No.  5. — Detailed  account  of  the 
electrolytic  formation  of  aluminum  hydrate 
in  Ohio  River  water.  Passivity  of  aluminum 
electrodes.  Rate  and  form  in  which  alu 
minum  leaves  the  positive  pole.  Form  and 
rate  of  deposition  of  aluminum  on  the  nega 
tive  pole.  Influence  of  the  composition  of 
the  river  water  on  the  formation  of  hydrate 
and  of  scales.  Influence  on  the  formation 
of  hydrate  of  the  presence  of  scale.  Influ 
ence  on  the  process  of  reversing  the  direc 
tion  of  the  electric  current.  Metal  wasted 
in  the  process.  Influence  of  scale  and  de 
posit  on  the  amount  of  power  required. 
Electric  power  wasted  in  the  process.  Con 
clusions. 

Section  No.  6. — Relative  efficiency  of 
available  coagulants.  General  review  of 
available  coagulants.  Relative  efficiency 
in  connection  with  24  hours'  subsidence, 
of  sulphate  of  alumina  and  sulphate  of 
iron  ;  persulphate  of  iron  and  electric 
current  with  iron  electrodes,  and  sulphate 
of  alumina  and  electric  current  with  alu 
minum  electrodes.  Relative  efficiency  in 
connection  with  filtration,  of  sulphate  of 
alumina  and  persulphate  of  iron;  sulphate  of 
alumina  and  electric  current  with  iron  elec 
trodes;  and  sulphate  of  alumina  and  electric 
current  with  aluminum  electrodes.  Conclu 
sions. 

Section  No.  7. —  Economical  application  of 
coagulants  to  aid  in  the  removal  of  sus 
pended  matter  by  sedimentation.  Relative 


TABLE   OF  CONTENTS. 


efficiencies  in  sedimentation  of  different 
amounts  of  coagulants. 

Section  No.  8. —  Effect  of  the  period  of  co 
agulation  of  the  river  water  before  filtration 
on  the  results  of  filtration. 

Section  No.  9. — Degree  of  coagulation  of 
the  water  before  filtration,  and  the  minimum 
amount  of  coagulant  required  for  that  pur 
pose. 

Section  No.  10. — The  conditions  of  suc 
cessful  filtration  by  the  American  system. 
Amount  of  suspended  matter  in  the  water 
reaching  the  sand  layer  and  the  coagulation 
of  the  same.  Rate  of  filtration.  Available 
head — negative  and  positive.  Cleaning  the 
sand  layer.  Application  of  caustic  soda. 
Character  of  the  sand  layer. 

Section  No.  u.  —  Quality  of  the  efflu 
ent  after  proper  sedimentation,  coagula 
tion,  and  filtration,  independent  of  the  na 
ture  of  the  coagulant.  Appearance.  Taste 
and  odor.  Organic  matter.  Mineral  mat 
ter.  Gases.  Algae  and  other  micro-or 
ganisms.  Bacteria.  Undecomposed  coag 
ulants.  Storage  of  effluent.  Corrosion  of 
rnetal  receptacles  by  the  effluent.  Loss  of  the 
partial  protective  influence  of  the  suspended 
matter  in  the  river  water  against  corrosion. 
Adaptability  of  the  effluent  for  boiler  use. 
Uniformity  in  quality  of  the  effluent. 

Section  No.  12. —  Manner  in  which  the 
nature  of  the  coagulant  affected  the  quality 
of  the  effluent. 

Section  No.  13. — Amounts  of  the  differ 
ent  available  coagulants  which  would  be  re 
quired,  with  optimum  conditions  of  sub 
sidence  and  filtration,  to  purify  satisfactorily 
the  Ohio  River  water. 

Section  No.  14. — Degree  to  which  the  sev 
eral  coagulants  in  their  respective  amounts 
would  affect  the  quality  of  the  effluent,  with 
its  practical  significance,  and  a  consideration 
of  the  advisability  and  cost  of  the  removal 
of  the  added  constituents. 

Section  No.  15. — Comparative  costs  of 
equivalent  amounts  of  the  available  coagu 
lants,  and  an  estimate  of  the  yearly  cost  of 
treatment  of  the  Ohio  River  water  by  each  of 
them. 


CHAPTER  XVI. 
FINAL  SUMMARY    AND  CONCLUSIONS 438 

Character  of  the  unpurified  Ohio  River 
water.  Applicability  to  the  purification  of 
the  Ohio  River  water  of  the  three  methods 
investigated  during  these  tests.  Imperative 
ness  of  the  use  of  coagulants.  Relative 
adaptability  of  American  and  English  types 
of  filters.  Removal  of  coarse  matters  by 
plain  subsidence.  Most  suitable  coagulant 
for  use  with  the  Ohio  River  water.  Prepa 
ration  and  application  of  solutions  of  sul 
phate  of  alumina.  Coagulation  and  subsid 
ence.  Coagulation  and  filtration.  The  op 
timum  period  of  coagulation.  Total  annual 
average  amounts  of  sulphate  of  alumina  re 
quired  for  coagulation.  Filtration.  Essen 
tial  features  of  an  American  filter  for  the 
successful  filtration  of  25  million  gallons  of 
Ohio  River  water  daily.  Quality  of  the 
purified  Ohio  River  water.  Final  conclu 
sions. 

APPENDIX. 

Technical  description  of  methods  used  for 
the  collection  of  samples  and  of  the  princi 
pal  features  in  the  methods  of  analyses. 

Tables  for  the  conversion  of  the  various 
unit  quantities  employed 445 

ILLUSTRATIONS. 

Plate  No.         I.     Plan  of   Grounds  of  Exper 
imental  Station. 
"        "         II.     Plan     of    Warren     Gravity 

System. 
"         "       III.     Section  of  Warren    Gravity 

System. 
IV.     Plan     of      Jewell      Gravity 

System. 
"        "         V.      Section    of    Jewell    Gravity 

System. 
"        "       VI.     Plan    of    Western    Pressure 

and  Gravity  Systems. 
"        "      VII.     Section  of  Western  Pressure 

and  Gravity  Systems. 
"        "    VIII.     Typical    Areas    of    Strainer 

Floors. 


WATER    PURIFICATION    AT    LOUISVILLE. 


TO    THE    PRESIDENT    AND    DIREC 
TORS   OF   THE   LOUISVILLE 
WATER   COMPANY. 

GENTLEMEN: 

Herewith  is  presented  the  full  report  of 
your  representative  upon  the  results  accom 
plished  during  the  recent  tests  by  the  several 
filters  or  systems  in  the  purification  of  the 
Ohio  River  water,  together  with  such  de 
scriptions,  comments,  and  conclusions  as  are 
deemed  pertinent  to  the  subject. 

The  following  niters  or  systems  of  water 
purification  were  investigated,  named  in  the 
order  in  which  they  were  installed  at  the 
pumping  station  of  this  Company,  where  the 
tests  and  investigations  were  conducted: 

1.  The  Jewell  Eilter,  of  the  O.  H.  Jewell 
Filter  Company,  73  Jackson  St.,  Chicago,  111. 

2.  The  Warren  Filter,  of  the  Cumberland 
Manufacturing    Company,    220    Devonshire 
St.,  Boston,  Mass. 

3.  The    Western    Gravity    Filter,    of    the 
Western  Filter  Company,  St.  Louis,  Mo. 

4.  The   Western    Pressure    Filter,    of   the 
Western  Filter  Company,  St.  Louis,  Mo. 

5.  The   Harris   Magneto-Electric   System, 
of  the  John  T.    Harris   Company,   of   New 
York  City. 

6.  The  Palmer  and  Brownell  Water  Puri 
fier,  of  Palmer  and  Brownell,  Louisville,  Ky. 

7.  The   MacDougall    Polarite   System,    of 
John  MacDougall,  Montreal,  Canada. 

On  Oct.  I,  1895,  the  writer  took  charge 
of  the  tests  and  investigations,  which  had  for 
their  purpose  the  determination  of  the  quality 
of  the  river  water  after  purification  on  a  prac 


tical  scale  by  each  of  the  filters  or  systems, 
and  the  collection  and  compilation  of  such 
data  as  would  indicate  the  cost  of  construc 
tion  and  operation  of  these  filters  or  systems 
of  purification.  The  first  three  weeks  were 
devoted  chiefly  to  the  construction  and  equip 
ment  of  a  suitable  laboratory,  in  which  chemi 
cal,  bacteriological,  and  microscopical  analy 
ses  of  the  water  could  be  made  after  the  most 
approved  methods. 

From  Oct.  21,  1895,  to  Aug.  i,  1896,  daily 
tests  were  made,  practically  without  interrup 
tion,  of  the  filters  or  systems  which  were  then 
ready.  On  Oct.  21,  1895,  tlle  Jewell  and 
Warren  filters  were  the  only  ones  in  readi 
ness  for  operation.  The  two  Western  filters 
were  tested  beginning  December  23,  1895 — 
the  date  when  their  construction  was  com 
pleted.  No  tests  were  made  of  the  Harris 
system  until  June  24,  1896,  when  it  was  first 
offered  for  official  inspection. 

The  greater  part  of  the  month  of  August, 
1896,  was  devoted  to  an  investigation  by  the 
Water  Company  into  the  practicability  of  the 
principles  employed  in  certain  devices  op 
erated  by  the  Harris  Company  during  the 
preceding  month.  This  was  made  necessary 
by  the  incompleteness  of  the  evidence  which 
had  been  accumulated  upon  this  point  by 
Aug.  i,  the  close  of  the  tests  as  originally 
provided  for. 

September,  October,  and  November,  1896, 
were  occupied  in  the  preparation  of  this  re 
port,  so  far  as  it  relates  to  work  done  up  to 
that  time. 

In  December,  1896,  special  tests  and  inves 
tigations  were  made  relating  to  the  action  of 


WATER  PURIFICATION  AT  LOUISVILLE. 


purified  water  in  the  corrosion  of  boilers  and 
pipes,  and  in  the  incrustation  of  steam-boilers. 
An  examination  was  also  made  of  an  experi 
mental  electrolytical  device  for  water  purifi 
cation,  submitted  for  inspection  to  the  Water 
Company  by  Profs.  Palmer  and  Brownell  in 
their  laboratory  at  the  Louisville  Manual 
Training  High  School. 

From  January  i  to  March  10,  1897,  at 
tention  was  given  to  the  construction  and  ex 
amination  of  electrolytical  devices  for  water 
purification,  designed  by  Profs.  Mark  and 
Brownell  of  Louisville,  and  to  the  investiga 
tion  of  points  of  practical  significance  con 
nected  therewith.  The  tests  of  these  elec 
trolytical  devices  were  the  outcome  of  the 
inspection  of  the  above-mentioned  laboratory 
experiments  made  by  Profs.  Palmer  and 
Brownell  in  December,  1896. 

When  the  tests  of  these  electrolytical  de 
vices  as  designed  by  Profs.  Mark  and  Brown 
ell  were  brought  to  a  close  on  March  10,  1897, 
it  had  been  decided  to  investigate  the  Mac- 
Dougall  Polarite  System  as  soon  as  a  test 
plant  could  be  constructed.  It  was  also  ar 
ranged  on  that  date  that  the  intervening  time, 
before  the  polarite  system  was  completed, 
should  be  occupied  in  constructing  and  test 
ing  devices  designed  by  the  officers  of  the 
Water  Company.  This  work,  which  was 
carried  on  solely  by  the  Water  Company,  was 
intended,  as  far  as  possible,  to  be  a  practical 
demonstration  of  some  of  the  leading  con 
clusions  drawn  from  the  foregoing  tests,  and 
to  extend  our  knowledge  along  several  im 
portant  but  not  thoroughly  understood  lines, 
so  far  as  time  permitted.  Owing  to  several 
unavoidable  delays,  the  construction  of  the 
devices  of  the  Water  Company  was  not  com 
pleted  until  April  10.  They  were  then  tested 
until  May  10,  when  the  MacDougall  Polarite 
System  was  offered  for  official  examination. 
This  system  was  tested  from  May  10  to  19, 
and  from  May  28  to  June  12,  inclusive. 

The  remainder  of  the  time  up  to  August  I, 
1897,  the  date  of  the  final  close  of  these  in 
vestigations,  was  devoted  to  work  upon  the 
devices  of  the  Water  Company  referred  to 
above. 

Since  August  i,  the  time  has  been  devoted 
to  the  preparation  of  this  report  so  far  as  it 
relates  to  work  done  after  January  i,  1897. 


NATURE  OF  THE  SYSTEMS  OF  PURIFICATION 
WHICH  WERE  TESTED. 

Before  recording  the  results  accomplished 
by  these  several  methods  of  purification  it  is 
necessary  to  show  in  general  terms  how  they 
differed  from  each  other  and  from  those 
which  have  been  employed  elsewhere.  At 
present  the  custom  prevails  to  a  large  extent 
of  calling  all  devices  for  water  purification  by 
the  name  of  filters.  In  a  majority  of  cases  fil 
tration  of  some  kind  is  employed  in  the 
process  of  purification,  but  none  of  the  de 
vices  tested  by  this  company  at  this  time 
consisted  of  plain  filtration,  as  the  term  is 
properly  used.  Filtration  alone  means  simply 
the  passage  of  the  water  taken  from  its  source 
through  a  layer  of  sand  or  similar  material. 
This  process,  which  is  briefly  outlined  in  the 
following  pages,  has  been  successfully  em 
ployed  for  many  years  in  Europe,  where  the 
yield  of  filtered  water  per  acre  of  filtering  sur 
face  is  about  2,000,000  gallons  per  24  hours. 
When  river  water,  which  contains  much  mud, 
clay,  and  other  suspended  matters,  reaches 
the  sand  layer,  the  pores  of  the  sand  become 
clogged  so  that  it  is  soon  necessary  to  scrape 
off  a  layer  of  the  surface  sand  and  accumula 
tions  which  are  deposited  on  it.  This  treat 
ment  would  apparently  be  required  at  frequent 
intervals  in  the  filtration  by  this  method  of  the 
Ohio  River  water  when  in  its  muddiest  con 
dition,  even  after  the  water  had  been  sub 
sided  for  several  days,  and  a  large  reserve 
area  would  probably  be  necessary  to  maintain 
the  city  supply.  The  cost  of  this  reserve 
area  of  filters,  and  of  the  scraping  of  the 
sand  surface,  would  probably  be  great  if  this 
method  were  adopted  here,  as  I  understand 
was  indicated  to  be  the  case  from  experiments 
made  by  your  Chief  Engineer,  Mr.  Charles 
Hermany,  at  the  Crescent  Hill  Reservoir  dur 
ing  the  summer  and  fall  of  1884  and  spring  of 
1885. 

In  the  systems  of  purification  which  were 
recently  tested  by  this  company  there  were 
tried  a  number  of  different  methods  that  were 
claimed  to  make  the  cost  of  purification 
less  than  by  sand  filtration,  such  as  has 
been  adopted  in  many  European  cities  in 
purifying  river  waters  less  muddy  than  that  of 
the  Ohio  River.  With  one  exception,  in  all 


IN  TROD  UCTION. 


of  these  systems  of  purification  filtration 
through  sand  or  quartz  was  made  a  very 
prominent  portion  of  their  respective  meth 
ods,  although  the  various  filters  were  con 
structed  and  operated  differently  from  those 
used  in  Europe.  But  the  principal 'difference 
between  the  European  method  of  filtration 
and  all  but  one  of  those  tested  at  Louisville 
lies  in  the  fact  that  in  these  test  systems  the 
water  was  coagulated  by  chemical  or  electro- 
lytical  treatment,  so  that  a  portion  of  the 
suspended  matter  could  settle  out  more  rap 
idly  in  basins  before  the  water  reached  the 
sand  layer;  and,  further,  so  that  the  water 
could  be  filtered  through  sand  about  fifty 
times  as  fast  asxwhen  no  coagulation  was 
afforded  the  water.  In  the  method  of  filtra 
tion  in  which  there  was  no  coagulation  of  the 
water  by  chemical  (or  electrolytical)  treat 
ment,  use  was  made  of  two  filters  for  the 
water  to  pass  through  in  turn,  and  this  second 
filter  contained  a  layer  of  material  called  po- 
larite,  in  addition  to  the  sand.  The  rate  of 
filtration  through  the  polarite  filter  was  about 
one-half  as  fast  as  through  those  filters  re 
ceiving  coagulated  water. 

THE  WARREN,  JEWELL,  WESTERN  GRAVITY, 
AND  WESTERN  PRESSURE  FILTERS. 

In  the  Warren,  Jewell,  Western  Gravity, 
and  Western  Pressure  Filters  the  general 
method  of  procedure  was  identical,  and  sub 
stantially  as  follows: 

Sulphate  of  alumina  (or  alum)  was  added  to 
the  river  water,  as  it  entered  the  devices  in  quan 
tities  varying  with  the  character  of  the  water. 
By  combining  with  lime  naturally  dissolved 
in  the  river  water  the  sulphate  of  alumina 
formed  a  white,  gelatinous,  solid  compound, 
called  hydrate  of  alumina.  This  latter  com 
pound  gradually  coagulated  the  suspended 
matter  in  the  river  water,  in  a  manner  similar 
to  the  well-known  action  of  white  of  egg  when 
added  to  turbid  coffee.  In  the  settling  basins, 
where  the  river  water  first  entered,  this  co 
agulation  progressed  so  that,  as  the  water  left 
the  settling  basins  and  entered  the  sand  layer, 
the  river  water  had  lost  some  of  the  mud  sus 
pended  in  it,  and  the  mud  and  clay  which  it 
did  contain  were  formed  into  flakes  of  suffi 
cient  size  to  allow  a  very  rapid  flow  of  water 


through  the  sand  layer,  with  satisfactory  re 
sults.  The  claim  that  this  method  of  water 
purification  was  more  economical  for  the 
Ohio  River  water  than  those  practised  in 
Europe  was  based  on  the  assertion  that  com 
paratively  small  amounts  of  sulphate  of  alu 
mina  permitted  a  very  great  reduction  in  the 
necessary  area  of  filtering  surface. 

While  in  the  general  method  of  procedure 
these  four  systems  were  the  same,  yet  they 
were  different  in  the  manner  in  which  the 
practical  details  were  carried  out.  That  is  to 
say,  there  were  different  devices  for  the  ap 
plication  of  sulphate  of  alumina;  the  settling 
basins  differed  in  size  and  arrangement;  and 
in  the  filters  themselves  the  sand  layers  were 
different  in  depth  and  size  of  grain,  and  were 
cleaned  in  somewhat  different  ways.  Detailed 
accounts  of  these  filters  are  given  beyond,  but 
these  statements  show  the  general  status  of 
the  matter.  It  may  also  be  added  here  that 
when  these  tests  were  begun  there  were  no 
means  of  telling  which  system  had  the  best 
practical  devices;  or,  indeed,  whether  any  of 
them  was  adapted  to  a  satisfactory  and 
reasonably  economical  purification  of  the 
Ohio  River  water  at  this  point. 

THE  HARRIS  DEVICE. 

In  the  Harris  Magneto-Electric  System  of 
water  purification,  which  was  tested  for  a 
short  period  in  June,  1896,  no  use  was  made 
of  filtration.  It  consisted  in  treating  the 
river  water  directly  with  an  electric  (spark) 
discharge,  and  the  subsequent  passage  of  the 
water  through  iron  tanks,  in  which  were  car 
bon  electrodes,  and  on  which  were  placed 
powerful  magnets.  The  electric  current  was 
supposed  to  destroy  the  germs  and  the  or 
ganic  matter,  while  the  mud,  clay,  and  silt 
were  to  be  separated  out  from  the  water  by 
the  repellent  action  of  the  magnets. 

In  July,  1896,  the  Harris  Company  made 
some  experiments  with  the  application  of 
electricity  to  the  purification  of  the  Ohio 
River  water  by  a  method  in  which  the  hy 
drate  of  alumina  (formed  in  the  case  of  the 
other  filters  by  the  decomposition  of  sulphate 
of  alumina  by  lime,  as  stated  above)  was  pre 
pared  by  the  electrolytic  decomposition  of 
metallic  aluminum.  It  was  apparently  the 


WATER  PURIFICATION  AT  LOUISVILLE. 


intention,  so  far  as  appliances  permitted,  to 
coagulate  the  water  by  the  same  chemical 
compound  as  in  the  sulphate  of  alumina  treat 
ment,  and  then  proceed  with  subsidence  and 
filtration  in  a  manner  similar  to  that  em 
ployed  in  the  case  of  the  other  filters,  the 
only  difference  in  the  methods  being  in  the 
manner  of  application  of  chemicals:  in  one 
case  a  commercial  chemical  product  was  em 
ployed,  while  in  the  other  case  the  coagulat 
ing  compound  was  made  by  the  electrolytic 
action  on  the  pure  metal.  Aside  from  the 
question  of  cost  the  electric  treatment  has 
certain  advantages,  which  will  be  explained 
subsequently. 

THE   MARK-BROWNKLL   DEVICES. 

During  the  months  of  January,  February, 
and  March,  1897,  electrolytical  devices,  de 
signed  by  Profs.  Mark  and  Brownell,  were 
constructed  and  tested.  These  devices  were 
an  improvement  in  several  ways  over  those 
of  the  Harris  Company.  Their  only  differ 
ence  in  general  method  was  the  substitution 
of  iron  electrodes  for  aluminum  electrodes. 
The  electric  current  produced  hydrate  of  iron, 
a  compound  similar  to  hydrate  of  alumina  in 
its  coagulating  properties,  and  it  was  claimed 
that  this  would  materially  reduce  the  cost  of 
purification. 

THE  MACDOUGALL  POLARITE  SYSTEM. 

The  results  of  the  tests  at  this  point  indi 
cated  the  desirability  of  reducing  the  amount 
of  the  coagulating  chemicals  whether  pro 
duced  electrolytically  or  from  commercial 
products,  and,  if  possible,  doing  away  with 
them  altogether.  It  was  claimed  by  Mr. 
MacDougall  that,  judging  from  experience  in 
purifying  the  water  of  the  river  Nile  and  of 
some  English  streams,  the  Ohio  River  water 
could  be  economically  purified,  without  the 
use  of  coagulating  chemicals,  by  his  polarite 
filter.  By  this  method  the  river  water  was 
passed  through  a  settling  tank  (replaced  later 
by  a  coke  strainer)  to  remove  the  coarsest 
matter,  thence  the  water  was  passed  at  a 
rapid  rate  through  a  sand  filter  in  order  to 
remove  further  the  particles  of  mud,  silt,  and 


clay.  The  partially  clarified  water  was  finally 
passed  at  a  slower  rate  through  a  filter  con 
taining  a  polarite  layer  with  sand  layers 
above  and  below  it.  This  polarite  is  an  iron 
ore  which  has  been  treated  by  a  patent  pro 
cess.  By  doing  away  with  the  use  of  coagu 
lating  chemicals,  and  their  attending  cost, 
and  at  the  same  time  securing  a  rate  of  filtra 
tion  many  times  greater  than  in  the  case  of 
plain  sand  filtration,  the  advantage  of  polar 
ite  as  a  filtering  material  was  claimed  to  be 
great.  The  polarite  filter  was  tested  from 
May  10  to  19,  and  May  28  to  June  12,  1897. 

METHODS    AND    DEVICES    OF    THE    WATER 
COMPANY. 

During  the  time  which  was  required  for 
the  construction  of  the  polarite  filter,  advan 
tage  was  taken  of  the  opportunity  for  the 
Water  Company  to  test  some  of  their  own 
plans  which  had  arisen  as  an  outcome  of  the 
foregoing  tests.  These  methods  and  plans 
are  described  fully  beyond,  in  Chapter  XV, 
but  their  objects  may  be  briefly  outlined  as 
follows: 

1.  A  reduction  in  the  cost  of  purification 
by  a  removal  of  the  bulk  of  the  mud,  silt,  and 
clay  from  the  river  water  before  it  reaches 
the  filters,  thereby  doing  away  with  the  ne 
cessity  of  a  large  reserve  portion  of  a  filter 
plant,   to   be   used   only   at   times   of   muddy 
water,  with  its  cost  of  installation  and  opera 
tion.     Experiments  upon  a  small  scale  with 
the  removal  of  the  bulk  of  the  mud  by  sub 
sidence    alone   were    made   during    the    early 
summer  of  1896,  and  gave  very  promising  re 
sults. 

2.  The     most     economical     and     efficient 
method  of  application  of  coagulating  chemi 
cals,  in  connection  with   subsidence,   to   pre 
pare  the  water  for  filtration  at  a  rapid  rate, 
with  reference  to  the  best  period  for  the  co 
agulation   of   the    matter    suspended    in    the 
water. 

3.  The  relative  economy,  advantages,  and 
disadvantages  of  different  coagulating  chemi 
cals  prepared  in  various  ways. 

The  investigations  along  these  lines  were 
carried  to  a  logical  end  so  far  as  was  con 
sidered  possible  under  the  existing  condi 
tions. 


IN  TROD  UCTION. 


THE  STATE  OF   DEVELOPMENT   OF  WATER 

PURIFICATION  AT  THE  TIME  OF 

THESE  TESTS. 

While  much  careful  attention  has  been 
given  to  the  art  of  water  purification  for  more 
than  sixty  years,  yet  the  general  solution  of 
the  problem  on  a  practical  basis  for  large 
cities  is  far  from  satisfactory  or  complete  at 
its  present  stage  of  development.  This  is 
due  partly  to  varying  effects  of  the  adopted 
processes  with  different  natural  waters,  partly 
to  the  lack  of  a  widely  practical  and  scientific 
understanding  of  the  influence  of  a  number  of 
factors  of  the  processes  themselves,  and  partly 
to  the  great  cost  involved  in  the  construc 
tion  of  adequate  filtration  works.  With  a 
river  water  of  such  exceedingly  great  varia 
tions  in  its  composition  as  that  of  the  Ohio 
River,  and  with  proprietary  systems  of  puri 
fication  about  which  so  little  accurate  in 
formation  was  available,  these  tests  at  Louis 
ville  were  bound  to  be  pioneer  work  in  a  large 
measure.  Nevertheless,  valuable  data  were 
obtained.  But  to  understand  the  significance 
of  these  data,  and  to  give  them  their  true 
value  in  the  line  of  studies  necessary  to 
place  this  line  of  work  on  a  satisfactory  basis 
and  capable  of  general  application,  it  is  essen 
tial  to  trace  the  development  of  this  subject 
up  to  this  time. 

BRIEF  HISTORICAL  RESUME. 

The  filtration  of  public  water  supplies  was 
first  adopted  at  London,  England.  The  date 
of  adoption  of  filtration  at  London  has  been 
generally  regarded  in  this  country  as  1839. 
But  it  is  now  known  that  a  sand  filter,  one 
acre  in  area,  was  put  in  service  in  1829,  the 
year  following  the  appointment  of  the  first 
Royal  Commission  on  the  Quality  of  the 
Metropolitan  Water  Supply.  This  Commis 
sion  recommended  the  filtration  of  the 
Thames  water,  and  the  filter  referred  to  above 
was  constructed  by  the  Chelsea  Water  Com 
pany  in  compliance  therewith. 

Progress  in  the  adoption  of  filtration  was 
slow  until  after  1849.  During  this  year  there 
was  a  severe  cholera  epidemic,  and  in  August, 
1849,  Dr.  Snow  first  formally  announced  the 
theory  that  drinking  water,  polluted"  from 


those  ill  or  dead  of  cholera,  was  the  chief 
means  of  propagation  of  this  disease.  Fol 
lowing  this  the  nitration  of  river-water  sup 
plies  advanced  less  slowly.  After  December 
31,  1855,  filtration  of  all  river  water  supplied 
to  the  Metropolitan  District  of  London  was 
made  compulsory  by  an  Act  of  Parliament 
passed  in  July,  1852. 

Since  this  date  rapid  advance  in  the  adop 
tion  of  filtration  for  public  water  supplies  has 
been  made  in  Europe.  The  population  of 
the  European  cities  now  supplied  with  fil 
tered  water  aggregates  from  fifteen  to  twenty 
millions,  or  more.  After  the  severe  epidemic 
of  cholera  at  Hamburg  in  1892,  caused 
largely  by  the  polluted  Elbe  water,  the  Im 
perial  Board  of  Health  of  Germany  ordered 
that  all  public  water  supplies  in  that  country 
drawn  from  rivers  or  lakes  should  be  filtered. 

During  the  last  thirty  years  there  has  been 
a  marked  increase  in  the  efficiency  of  these 
systems  of  purification  of  European  water 
supplies,  owing  to  improvements  in  both  the 
construction  and  the  operation  of  the  filters. 
The  first  important  step  in  this  direction  was 
taken  at  London  in  1871,  when  Parliament 
made  provision  for  systematic  examinations 
at  frequent  intervals  of  the  filters  and  the  fil 
tered  water.  The  greatest  progress,  how 
ever,  has  been  made  during  the  past  dozen 
years.  This  has  been  due  to  the  establish 
ment  of  the  germ  theory  of  disease,  and  the 
general  recognition  by  sanitarians  that  such 
diseases  as  typhoid  fever  and  cholera  are 
transmitted  largely  by  drinking  water.  And, 
further,  rapid  developments  in  the  new  science 
of  bacteriology  have  made  it  possible  to  apply 
this  science  in  the  solution  of  problems  in 
water  purification,  so  as  to  yield  results  of 
substantial  and  practical  value. 

The  recognition  of  the  need  of  reliable  in 
formation  from  an  engineering,  chemical,  and 
bacteriological  standpoint  to  facilitate  the 
adoption,  construction,  and  operation  of  puri 
fication  systems  has  led  to  several  important 
investigations.  These  have  been  made  in 
England,  Germany,  and  America. 

One  of  the  objects  of  filtration,  in  many 
instances  in  Europe,  has  been  to  remove  mud, 
silt,  and  clay  from  river  water.  In  many 
cases,  however,  filtration  has  also  been  di 
rected  to  protect  the  water  consumers  from 


WATER   PURIFICATION  AT  LOUISVILLE. 


those  diseases  which  are  carried  by  the  water. 
This  is  a  very  important  matter  in  Europe, 
where  the  population  has  become  very  dense 
around  the  great  cities.  In  America,  with  its 
comparatively  sparse  population,  it  is  not  as 
a  rule  so  pressing  at  present.  But  disastrous 
experience  in  Europe  with  some  filters  built 
in  the  early  days  of  water  purification  show 
clearly  that  all  niters  should  be  capable  at  all 
times  of  protecting  the  health  of  the  con 
sumers  from  water-borne  diseases. 


GENERAL   DESCRIPTION   OF   THE   MOST   IM 
PORTANT  TYPE  OF  FILTERS  ABROAD. 

Filters  such  as  were  introduced  into  Eng 
land,  and  which  have  since  been  employed 
regularly  there  and  in  many  places  "on  the 
Continent,  consist  substantially  of  a  large, 
open  basin  ranging  as  a  rule  from  about  0.5 
to  1.5  acres  in  area  and  jo  feet  or  more  in 
depth.  In  cold  climates,  such  as  in  Northern 
Germany,  they  are  covered,  to  afford  protec 
tion  from  ice  and  frost.  The  bottom  of  the 
basins  are  made  practically  water-tight.  On 
the  bottom  of  these  basins,  drains  and  pipes 
are  suitably  arranged  so  as  to-  conduct  the 
water  from  the  filter  to  a  collecting  well  or 
reservoir,  located  at  some  convenient  place 
near  the  filter.  In  some  cases,  instead  of 
using  lateral  pipes  with  perforations  or  open 
joints,  the  water  is  taken  to  the  main  tinder- 
drain  through  an  arrangement  of  dry-laid 
bricks.  , 

Over  the  underdrains  are  placed  succes 
sively  layers  of  broken  stone  and  gravel,  the 
depth  of  each  of  which  varies  usually  accord 
ing  to  the  construction  of  the  underdrains. 
The  size  of  the  stone  and  gravel  in  turn  be 
comes  gradually  finer  toward  the  top,  in  or 
der  that  they  may  better  serve  their  purpose 
of  supporting  the  layer  of  sand  which  rests 
upon  the  gravel.  The  thickness  of  this  layer 
of  sand  placed  upon  the  gravel  varies  in  dif 
ferent  filters  from  about  2  to  5  feet.  There 
is  also  some  variation  in  the  size  ot  the 
sand  grains  in  the  filters  of  the  different 
cities. 

In  the  operation  of  the  filters  water  flows 
or  is  pumped  from  the  river  or  sedimentation 
basin  onto  the  filter,  and  stands  several  feet 


in  depth  above  the  surface  of  the  sand.  The 
water  passes  downward  through  the  sand, 
gravel,  and  broken  stone,  in  turn,  and  thence 
through  the  underdrains,  collecting  well,  or 
reservoir,  and  pumps  (if  such  are  necessary) 
to  the  consumer.  The  rate  at  which  the 
water  Hows  by  gravity  through  the  filter  is 
generally  controlled  and  made  fairly  uniform 
by  regulating  devices  on  the  outlet  pipe  from 
the  filter. 

After  a  time,  when  a  geater  or  less  quan 
tity  of  water  has  passed  through  the  filter, 
there  appears  at  and  near  the  surface  of  the 
sand  an  accumulation  of  silt  and  other  mat 
ters  which  were  suspended  in  the  water  when 
it  reached  the  filter.  Eventually  this  accumu 
lation  becomes  so  great  that  the  interstices  of 
the  sand  are  clogged  so  that  an  adequate 
quantity  of  water  cannot  pass  through  the 
filter.  When  this  condition  of  affairs  obtains 
the  inlet  water  is  shut  off.  The  water  stand 
ing  on  the  filter  is  allowed  to  drain  to  some 
distance  below  the  surface  of  the  sand,  and 
workmen  remove  with  shovels  and  wheel 
barrows  the  upper  layer  of  the  clogged 
sand  ordinarily  to  a  depth  of  about 
0.5  to  0.75  inch.  The  main  body  of 
the  sand  is  cleaned  only  by  the  re 
moval  of  organic  matter  through  the  action 
of  bacteria.  The  filter  is  slowly  filled  with 
water  after  the  surface  has  been  scraped, 
either  by  applying  the  unfiltered  water  at  the 
top  or  by  letting  filtered  water  flow  in  from 
below.  This  latter  procedure,  where  the  con 
struction  of  the  filter  will  permit  it,  is  much 
the  better,  because  it  tends  to  prevent  the 
formation  of  channels  in  the  sand,  due  to  the 
escaping  air  which  enters  the  pores  of  the 
sand  upon  draining.  Such  channels  are  very 
objectionable,  because  they  allow  the  water 
to  pass  through  them  without  satisfactory  pu 
rification. 

Once  or  twice  a  year  the  layer  of  sand  is 
restored  to  its  original  thickness  by  either 
replacing  the  removed  sand  after  thorough 
washing,  or  adding  new  clean  sand.  In  some 
of  the  important  filters  of  this  type  use  is 
made  of  coagulating  chemicals,  but  the  rate 
of  filtration  is  comparatively  slow — about 
2,000,000  gallons  per  acre  daily.  In  Holland 
chemicals  for  coagulation  have  been  used  to 
some  extent. 


INTRODUCTION. 


PRINCIPLES  OF  SAND  FILTRATION  WITHOUT 
THE  USE  OF  COAGULATING  CHEMICALS. 

There  has  never  yet  been  given  an  accurate 
and  concise  definition  of  the  principles  by 
which  water  is  purified  by  the  type  of  filters  just 
described.  The  reason  of  this  appears  to  be 
that  there  are  several  factors  which  have  to  be 
taken  into  consideration;  and  the  relative 
practical  value  of  these  factors  seems  to  vary 
under  different  local  conditions.  As  we  now 
understand  the  subject,  the  principles  of  puri 
fication  by  this  type  of  filtration  involve  three 
significant  phases,  namely: 

A.  Mechanical  or  Physical. 

B.  Biological. 

C.  Chemical. 

A.  Mechanical  or  Physical. — There  are   at 
least  two  important  actions  of  a  mechanical 
or  physical  nature  which  aid  in  the  purifica 
tion    of    water    by    this    type    of    filtration, 
namely : 

1.  A  straining  action,  by  which  there  are 
removed    from   the    water   those    small    sus 
pended  particles  which  may  be  called  large 
when  compared  with  the  size  of  the  inter 
stices  in  the  sand  layer. 

2.  An  adhesive  action,  by  which  there  are 
removed  those  suspended  particles,  including 
the  bacteria,  which  are  far  smaller  than  the 
interstices  of  the  sand  layer  through  which 
the  water  passes. 

This  very  important  adhesive  action  is  in 
fluenced  by  several  varying  factors  and  is 
not  thoroughly  understood.  Its  efficiency  in 
filtration,  furthermore,  is  associated  to  a  con 
siderable  degree  with  chemical  and  biological 
conditions,  as  noted  below. 

B.  Biological. — This  aspect   is  of  practical 
significance  by  virtue  of  its  action  in  remov 
ing  organic  matter  which,  in  places  beneath 
the    upper    surface,    accumulates    as     films 
around  the  sand  grains.      The  removal  of  or 
ganic  matter  by  oxidation   and   nitrification 
appears  to  be  a  factor  in  causing  indirectly 
the  death  of  bacteria,  which  are  mechanically 
arrested  by  the  adhesive  action  of  the  sand 
grains.      By  some  it  has  been  claimed  that 
the  bacteria  pass  into  a  gelatinous  form,  the 
zoogloea  stage;    and,  being  attached  to  the 
sand   grains,   they   facilitate   thereby   the   re 
moval    of   bacteria    in    the    active    vegetable 


stage,  and  of  minute  suspended  particles  by 
means  of  adhesion. 

C.  Chemical. — The  chemical  side  of  filtra 
tion  deals  with  the  removal  of  dissolved  or 
ganic  matters  and,  together  with  the  bacteria, 
with  the  removal  of  organic  matters,  accumu 
lated  on  the  sand  grains.  In  many  cases  it 
appears  that  an  action,  more  or  less  chemical 
in  its  nature,  between  certain  ingredients  in 
the  water  and  certain  ingredients  of  the  sand 
causes  the  formation  of  films,  containing  or 
ganic  matter,  around  the  sand  grains.  This 
facilitates  the  mechanical  removal  from  water 
of  bacteria  by  the  adhesive  action  mentioned 
above;  and  it  is  also  probable  that  this  puts 
the  organic  matter  in  a  position  where  the 
bacteria  may  do  their  work  of  destroying  it 
to  better  advantage. 

In  the  early  days  of  filtration  the  mechani 
cal  and  chemical  aspects  of  the  subject  were 
the  only  ones  which  received  attention.  Since 
the  dawn  of  bacteriology  much  attention  has 
been  given  to  the  question  as  to  how  far  the 
biological  side  aided  in  the  accomplishment 
of  purification  by  filtration.  Biological  theo 
ries  advanced  rapidly.  By  some  it  was 
claimed  that  the  whole  process  was  a  bio 
logical  one.  These  theories,  however, 
reached  a  point  which  was  untenable,  and 
for  several  years  the  mechanical  and  chemical 
phases  have  been  regaining  more  nearly  their 
true  significance. 

ENGLISH  FILTERS. 

The  type  of  filters  which  we  have  been  con 
sidering,  and  which  was  introduced  at  Lon 
don,  England,  by  James  Simpson  in  1829,  is 
called  by  various  names.  The  number  has 
become  so  great  that  they  are  very  confusing. 
The  principal  names  given  to  this  type  of  fil 
ters  are  as  follows: 

1.  Filter  beds. 

2.  Sand  beds. 

3.  Sand  filters. 

4.  Artificial  sand  filters. 

5.  Natural  sand  filters. 

6.  Slow  sand  filters. 

7.  Biological  filters. 

8.  English  filters. 

9.  European  filters. 

Of  these  various  names  all  have  more  01 


WATER   PURIFICATION  AT  LOUISVILLE. 


less  significance,  although  some  of  them  con 
vey  an  impression  which  is  not  altogether 
correct.  Thus,  "  biological  filter "  in  the 
light  of  our  present  knowledge  is  an  unfor 
tunate  name,  because  it  gives  undue  promi 
nence  to  one  of  several  phases  of  the  process. 
Quite  recently  "  natural  sand  filters "  has 
been  used  by  many  to  designate  this  type  of 
filters.  This  expression  has  considerable 
significance  in  that  there  is  imitated  in  these 
filters  the  process  in  nature  by  which  spring 
water  and  other  ground  waters  are  purified 
by  filtration  through  the  upper  layers  of  the 
earth.  The  use  of  this  name  is  not  strictly 
correct  in  this  connection,  because  these  fil 
ters  are  actually  of  artificial  construction,  and 
the  processes  go  on  under  conditions  widely 
different  from  those  in  nature.  Natural  fil 
tration  for  public  water  supplies  is  correctly 
applied  only  to  those  cases  where  galleries  or 
wells  are  located  in  the  earth  near  a  river  or 
lake,  where  the  water  is  naturally  filtered, 
either  from  the  adjoining  body  of  water  or, 
more  frequently,  from  the  ground  on  the  land 
side,  where  it  is  naturally  filtered  through  the 
earth  before  it  reaches  the  place  of  collection. 
Natural  filters  as  thus  described  are  success 
fully  used  in  France  and  in  some  places  in  this 
country  where  the  geological  conditions  are 
favorable.  The  water  obtained  from  driven 
wells  is  also  similarly  purified. 

It  seems  practically  impossible  to  find  a 
name  which  will  specifically  characterize  the 
construction  and  operation  of  this  type  of  ni 
ter,  now  that  so  many  modifications  in  filters 
have  been  introduced.  In  view  of  this  fact, 
it  is  believed  that  "  English  filters  "  is  the  best 
name  to  apply  to  them,  and  we  shall  use  this 
name  throughout  this  report.  This  type  of 
filter  is  distinctly  of  English  origin,  and  Eng 
lish  engineers  and  English  capital  introduced 
it  on  the  Continent  of  Europe  at  an  early 
date,  at  Berlin,  St.  Petersburg,  Altona,  and 
other  places.  For  this  reason  and  the  fact 
that  there  are  several  modifications  in  some 
of  the  Continental  filters  we  prefer  to  call 
them  English  rather  than  European  filters. 

MODIFICATIONS  IN  EUROPE  OF  THE  ORIGI 
NAL  ENGLISH   FILTERS. 

In   England  there  have  been  no   marked 


changes  in  the  construction  of  filters,  al 
though  some  attempts  have  been  made  to  re 
place  sand  with  other  materials,  such  as 
carbide  of  iron,  and  polarite.  Improvements 
in  the  efficiency  of  filtration  for  the  most  part 
have  come,  however,  from  more  careful  op 
eration,  and  from  extensions  in  the  sedimen 
tation  basins.  In  the  latter  instance  there  is 
a  notable  reduction  in  the  cost  of  filtration  of 
turbid  and  muddy  river  waters. 

On  the  Continent  of  Europe,  however,  a 
number  of  modifications  in  the  original  filters 
have  been  introduced.  The  more  important 
ones  are  as  follows: 

Tours,  France. — In  1856  two  filters  were, 
put  in  service  at  this  place.  They  were  de 
signed  with  the  view  to  having  the  accumu 
lation  of  mud,  etc.,  on  the  surface  of  the  sand 
removed  by  forcing  filtered  water  up  through 
the  sand  from  the  bottom,  instead  of  having 
it  scraped  off  with  shovels  as  in  English  fil 
ters.  This  idea  never  worked  well  in  practice 
at  this  place,  owing  to  insufficient  pressure  to 
force  the  water  up  through  the  filter.  These 
filters  were  abandoned  after  a  time,  owing  ap 
parently  to  a  failure  to  provide  sedimentation 
basins  in  which  the  sediment  in  the  river 
water  could  subside  by  gravity. 

Holland. — In  several  places  in  Holland, 
notably  at  Leeuwarden,  Groningen,  and 
Schiedam,  and  also  at  Antwerp,  in  Belgium, 
alum  has  been  used  at  times  to  aid  in  the  pu 
rification  of  colored  and  polluted  water  by 
English  filters.  The  practical  effect  of  the 
application  of  alum  is  entered  into  in  detail  in 
a  subsequent  portion  of  this  report,  and  it  is 
the  purpose  here  only  to  record  its  use  in 
Holland. 

Anderson  Process. — This  process  has  been 
in  use  more  or  less  regularly  for  some  years 
at  Antwerp,  Belgium,  and  in  some  small 
towns  in  Europe.  Quite  recently  a  large 
plant  has  been  installed  at  Paris,  France,  for 
the  purification  of  water  from  the  river  Seine. 

Essentially  this  process  consists  of  passing 
the  water  first  through  a  revolving  cylinder 
containing  iron  filings.  The  carbonic  acid 
in  the  water  dissolves  some  of  the  iron,  form 
ing  ferrous  carbonate.  By  the  air  con 
tained  in  the  water  this  salt  of  iron  is 
oxidized  more  or  less  rapidly  to  ferric  hy 
drate.  The  iron  when  changed  into  this 


INTRODUCTION. 


solid,  gelatinous  form  combines  with  much  of 
the  organic  matter,  and,  like  aluminum  hy 
drate  formed  from  alum  or  sulphate  of  alu 
mina,  coagulates  the  suspended  matter,  and 
makes  it  easier  to  filter  the  water  subse 
quently  through  English  filters. 

ENGLISH  FILTERS  IN  AMERICA. 

Although  there  are  ten  or  twelve  com 
paratively  small  filters  in  America,  more  or 
less  resembling  English  filters,  it  may  be 
safely  stated  that  this  system  of  water  purifi 
cation  has  never  become  well  established  in 
this  country.  Among  the  principal  reasons 
of  this  are  the  following: 

1.  The  question  of  cost. 

2.  The  general  absence  of  State  or  Federal 
Boards  constituted  with  adequate  authority 
to  enforce  the  protection  of  citizens  from  pol 
luted  water  supplies,  as  is  the  case  in  the  more 
thickly  populated  countries  of  Europe. 

3.  The  absence  of  severe  cholera  epidem 
ics,  such  as  have  led  a  number  of  European 
cities  to  adopt  filtration  with  haste. 

For  a  number  of  years  sufficient  informa 
tion  has  been  available  to  show  that  prac 
tically  any  water  may  be  satisfactorily  puri 
fied  by  English  filters,  provided  sufficient 
sedimentation  is  first  employed  in  the  case 
of  very  turbid  or  muddy  waters,  and  that  the 
rate  of  filtration  is  sufficiently  low.  With  re 
gard  to  the  question  of  expense,  however,  it 
has  been,  and  is  still,  difficult  to  estimate  even 
approximately  the  cost  of  construction  and 
operation  of  filters  which  will  purify  a  turbid 
or  muddy  water  satisfactorily.  The  reason 
of  this  is  that  the  various  elements  of  cost 
differ  widely  with  the  local  conditions,  and 
especially  with  the  character  of  the  water  to 
be  purified. 

There  are  two  noteworthy  points  to  be 
mentioned  in  connection  with  English  filters 
in  America.  In  the  first  place  this  type  of 
water  purification  was  well  described  in  a 
report  by  an  American  engineer.  This 
gentleman,  now  deceased,  was  Mr.  James  P. 
Kirkwood,  Chief  Engineer  of  the  Water  Com 
mission  of  St.  Louis,  Mo.  In  December,  1865, 
he  was  instruct edby.the  commissioners  to  pro 
ceed  to  Europe  and  examine  into  this  ques 
tion  of  water  filtration,  with  a  view  to  apply 


ing  this  information  in  connection  with  the 
purification  of  the  water  supply  of  St.  Louis. 
The  publication  of  the  report  made  a  very 
valuable  work  of  reference,  which  has  been 
used  by  both  American  and  European  en 
gineers.  The  work  was  of  such  a  high  grade 
that  it  was  translated  into  German  in  1876. 
In  it  there  are  several  important  suggestions 
which  have  led  to  improvements  in  the  con 
struction  and  operation  of  this  type  of  filters. 
The  most  noteworthy  of  these  points  are  that 
the  removal  of  mud  and  silt  from  the  water 
by  subsidence  in  basins  before  the  water 
reaches  the  filters  reduces  the  cost,  and  in 
creases  the  efficiency  of  filtration;  and,  fur 
ther,  that  the  efficiency  of  the  operation  is 
enhanced  by  maintaining  by  suitable  devices 
a  uniform  flow  of  water  through  the  filter. 

During  the  past  six  years,  furthermore,  the 
most  extensive  experimental  investigations 
upon  the  purification  of  water  by  slow  filtra 
tion  through  sand,  unaided  by  treatment  with 
a  coagulant,  have  been  made  in  America  at 
the  Lawrence  Experiment  Station  of  the 
State  Board  of  Health  of  Massachusetts. 
These  investigations  have  yielded  a  large 
fund  of  information  on  the  purification  of  such 
clear  but  polluted  waters  as  that  of  the  Mer- 
rimac  River. 

Another  factor  which  has  recently  served 
to  explain  in  part  the  slowness  with 
which  American  cities  have  adopted  puri 
fication  systems  for  their  water  supplies  is 
the  fact  that  there  has  appeared  in  America 
within  the  last  dozen  years  another  type 
of  water  filter.  This  type  of  filter  is 
described  below.  It  is  spoken  of  as  the 
"  mechanical,"  "  alum,"  and  "  rapid  sand  " 
filter.  None  of  these  names  is  particularly 
appropriate,  and  in  distinction  from  the  Eng 
lish  filters  we  shall  refer  to  it  as  the  American 
filter. 

Both  types  of  filters  unquestionably  pos 
sess  merit.  But  as  to  their  relative  merits 
for  the  purification  of  waters  in  general,  or  of 
any  particular  water,  we  have  little  or  no  in 
formation  to  guide  us.  In  the  absence  of 
facts  there  have  arisen  in  connection  with  the 
subject  numerous  statements  and  opinions, 
many  of  which  are  partisan  and  erroneous. 
This  unfortunate  state  of  affairs  has  recently 
done  much  to  retard  the  adoption  of  muni- 


WATER  PURIFICATION  AT  LOUISVILLE. 


cipal  systems  of  water  purification,  and  will 
probably  continue  to  do  so  until  reliable  com 
parable  data  are  available. 

AMERICAN  FILTERS. 

This  type  of  filters  is  the  outgrowth  of 
schemes  to  purify  water  for  industrial  and 
manufacturing  purposes.  Its  development 
up  to  this  time  has  been  tentative  to  a  marked 
degree,  and  has  been  in  the  hands  of  several 
competing  business  corporations.  In  1883 
it  first  attracted  the  attention  of  those  con 
nected  with  public  water  supplies.  At  that 
time  it  consisted  essentially  of  a  large  circular 
tank  in  which  there  was  a  layer  of  sand  sup 
ported  by  a  perforated  bottom.  Its  chief 
characteristic,  other  than  small  size,  in  dis 
tinction  from  English  filters,  was  the  fact  that 
the  sand  layer  was  cleansed  of  the  accumu 
lated  materials  removed  from  the  river  water 
by  forcing  water  under  pressure  up  through 
the  layer  of  sand.  In  this  respect  it  resem 
bled  the  filters  constructed  in  1856  at  Tours, 
in  France. 

Patents  were  taken  out  in  1884  to  cover  a 
modification  which  consisted  of  the  applica 
tion  of  alum,  a  salt  of  iron,  or  other  similar 
coagulating  chemical,  to  the  water,  just  be 
fore  it  passed  through  the  layer  of  sand.  The 
custom  of  applying  alum  to  coagulate  water, 
in  order  to  facilitate  the  removal  of  foreign 
matter,  has  been  practised  in  various  ways 
for  many  centuries  in  different  parts  of  the 
world,  and  the  description  of  it  in  scientific 
literature  began  about  seventy  years  ago. 
The  apparent  object  of  the  application  of 
chemicals  under  the  stated  conditions  are  un 
derstood  to  be  a  reduction  in  the  cost  of 
treatment,  by  doing  away  with  subsidence 
basins,  and  by  diminution  of  the  area  of  filter 
ing  surface. 

This  type  of  filters  was  first  employed  in 
the  treatment  of  a  public  water  supply  at 
Somerville,  N.  J.,  in  1885.  Since  that  time 
many  towns  and  small  cities  have  adopted 
systems  of  this  general  type.  At  present  it  is 
said  that  over  100  town  and  municipal  plants 
are  in  operation,  but  among  this  number  there 
are  none  for  large  cities. 

In  the  last  ten  years  many  modifications 
have  been  introduced  by  the  several  compet 


ing  companies.  These  modifications,  more  or 
less  protected  by  patents,  relate  for  the  most 
part  to  devices  for  supporting  the  sand  layer 
at  the  bottom;  the  introduction  of  filtered 
water  under  pressure  below  the  sand  layer, 
to  enable  the  filter  to  be  cleaned  by  a  reverse 
flow  of  water;  and  of  agitating  devices  to  stir 
the  sand  during  washing,  and  thus  aid  the 
cleansing  process.  In  the  present  filters  of 
the  several  companies  the  coagulating  chemi 
cals  are  applied  at  points  differently  located 
with  reference  to  the  sand  layer,  and  with 
varying  provisions  to  secure  not  only  more 
complete  coagulation,  but  also  to  effect  a  re 
moval  of  some  suspended  matter  before  the 
water  is  filtered.  To  this  general  account  of 
the  American  filters  it  may  be  added  that  a 
majority  of  them  are  gravity  filters — where 
the  water  tlows  by  gravity  through  a  sand 
layer  placed  in  an  open  tank.  In  some  cases, 
however,  pressure  filters  are  used.  The  pres 
sure  filters,  in  addition  to  customary  devices, 
consist  of  a  sand  layer  placed  in  a  closed 
compartment,  so  that  the  water  can  be  forced 
through  the  filter  under  pressure,  thereby 
avoiding,  it  is  claimed,  additional  pumping 
under  some  conditions. 

Compared  with  the  English  filters,  the 
American  filters  at  present  show  the  follow 
ing  principal  differences: 

T.  The  American  filters  are  aided  by  the 
application  to  the  water  of  a  coagulating 
chemical,  which  makes  it  possible  to  filter 
through  sand  at  a  much  more  rapid  rate,  and 
thereby  the  necessary  area  of  filter  is  much 
reduced. 

2.  The  American  filters  are  cleaned  In- 
passing  a  stream  of  water  upward  through 
the  sand,  with  or  without  accompanying  agi 
tation,  rather  than  by  scraping  off  the  surface 
layers,  as  in  the  case  of  the  English  filters. 

There  are  of  course  many  other  features 
of  difference,  such,  for  example,  as  the  strain 
ers  at  the  bottom,  to  hold  back  the  sand,  and 
at  the  same  time  furnish  an  exit  for  the  fil 
tered  water;  but  the  two  points  stated  above 
are  the  principal  differences. 

EFFICIENCY    OF    AMERICAN    FILTERS,    AND 
COST  OF  THEIR  OPERATION. 

At   the   beginning  of  the   Louisville  tests 


INTRODUCTION. 


there  were  no  available  data  which  would 
show  whether  or  not  the  American  type  of 
filter  was  capable  of  purifying  the  Ohio  River 
water;  or  which  of  the  several  companies  had 
the  best  filter  for  sale;  or  whether  any  of  the 
American  filters  were  capable  of  purifying;  the 
Ohio  River  water  at  a  reasonable  cost.  It  is 
true  that  some  scattering  data  indicated  a 
satisfactory  purification  of  certain  waters  by  this 
type  of  filters,  but  there  was  other  information 
pointing  to  work  of  an  inferior  grade.  With 
regard  to  the  question  of  cost,  practically 
nothing  was  available  which  would  be  of  any 
service  in  considering  the  purification  of  such 
an  exceedingly  variable  water  as  that  of  the 
Ohio  River.  On  the  one  hand,  it  was  claimed 
that  somewhat  similar  muddy  waters  were 
purified  at  a  comparatively  low  cost  by  this 
type  of  filter;  while,  on  the  other  hand,  it  was 
known  that  a  system  of  purification  installed 
at  New  Orleans  by  one  of  the  prominent 
American  filter-makers  had  for  some  reason 
been  a  failure.  What  the  exact  facts  and  con 
ditions  of  purification  were  at  the  several 
places  where  this  type  of  filter  had  been  tried 
could  not  be  learned.  In  fact  there  is  reason 
to  believe  that  they  were  not  accurately 
known. 

Very  early  in  these  tests  the  results  of  some 
tests  of  an  American  filter  made  at  Provi 
dence,  R.  I.,  were  available.  The  Providence 
work  was  of  much  value  in  indicating  that  it 
was  possible  with  some  waters  and  some  con 
ditions  to  accomplish  a  satisfactory  purifica 
tion  by  this  type  of  filter.  But  the  Pawtuxet 
River  water,  so  far  as  can  be  learned  from  the 
limited  analytical  evidence  as  to  its  character, 
is  very  much  easier  to  purify  than  the  Ohio 
River  water.  And  it  may  be  safely  stated  that 
a  thoroughly  satisfactory  solution  of  the  prob 
lem  of  purifying  the  Pawtuxet  water  could 
not  by  any  means  serve  as  an  adequate  guide 
for  the  purification  of  the  Ohio  water.  An 
attempt  was  also  made  to  learn  the  relative 
advantages  of  the  English  and  American 
types  of  filters  in  purifying  the  local  water, 
but  the  conditions  were  such  that  in  this  re 
spect  the  work  at  Providence  led  to  no  de 
cisive  conclusions  of  value. 

With  regard  to  the  Harm  Magneto-Elec 
tric  System  it  was  said  that  an  experimental 
device  at  Brooklyn  had  been  successful  in  pu 


rifying  the  local  water,  but  no  accurate  idea 
could  be  obtained  as  to  the  cost  of  treatment. 

The  Mark  and  Brownellelectrolytical  device, 
in  which  the  current  of  electricity  was  applied 
to  the  water  through  iron  electrodes,  was  on 
the  same  principle  as  the  Webster  Process  for 
sewage  purification.  Eight  or  nine  years  ago 
the  Webster  Process  was  claimed  in  England 
to  be  very  promising,  but  for  the  past  few 
years  little  or  nothing  had  been  heard  about 
it.  As  already  stated,  this  electrolytical  de 
vice  replaces  the  application  of  chemicals,  but 
it  was  used  in  connection  with  American  fil 
ters.  This  portion  of  the  test,  therefore,  re 
fers  to  the  coagulation  preceding  filtration. 
The  MacDougall  Polarite  System  had  never 
been  tried  in  America,  but  fragmentary  ac 
counts  of  its  trial  in  England  and  Egypt  in 
dicated  that  it  probably  had  some  advantages. 

Such  were  the  conditions  found  by  the 
Louisville  Water  Company  when  they  made 
these  tests,  with  a  view  to  finding  a  practi 
cable  method  of  purifying  the  Ohio  River 
water  as  delivered  to  the  citizens  of  Louis 
ville. 

CONDITIONS  UNDER  WHICH  THE  TESTS  WERE 
CONDUCTED. 

The  investigations  and  tests  described  in 
the  following  portion  of  this  report  were  all 
conducted  at  the  pumping  station  of  the 
Water  Company,  about  three  miles  above  the 
city  of  Louisville  on  the  Kentucky  shore  of 
the  Ohio  River.  A  plan  of  the  ground  at  the 
pumping  station  is  presented  on  Plate  I. 

The  Water  Company  constructed  six  tem 
porary  buildings,  four  of  which  were  occupied 
by  the  companies  which  offered  purification 
systems  for  examination.  One  of  them  was 
equipped  as  the  laboratory  of  the  Water 
Company,  and  under  the  direction  of  the 
writer  was  furnished  with  all  apparatus  and 
supplies  necessary  for  analytical  work  in  tin's 
line  after  the  best  modern  methods.  The 
remaining  building  contained  a  pump  with 
which  filtered  water  under  pressure  was  sup 
plied  for  washing  the  filters.  Steam,  and 
Ohio  River  water  taken  from  the  force  main 
at  a  point  about  390  feet  from  the  intake,  were 
supplied  by  the  Water  Company  to  these 
buildings.  All  the  piping  leading  to  and  from 


WATER   PURIFICATION  AT  LOUISVILLE. 


the  buildings,  the  meters  on  the  water-pipes, 
and  sewer  connections  were  also  furnished  by 
the  Water  Company. 

During  the  period  preceding  Aug.  i,  1896, 
the  four  buildings  above  mentioned  were  oc 
cupied  by  the  Warren  Filter,  the  Jewell  Fil 
ter,  the  two  Western  Filters,  and  the  Harris 
Magneto-Electric  System  of  purification,  re 
spectively,  named  in  the  order  of  their  loca 
tion,  beginning  at  the  laboratory.  This  order 
was  used  in  the  current  note-books,  and  as  a 
matter  of  convenience  the  several  systems  of 
purification  will  be  referred  to  in  this  report 
in  the  above  order.  In  view  of  the  fact  that 
filtration  alone  was  not  the  only  method  em 
ployed  in  the  purification  processes,  the  term 
system  of  purification  will  be  used  in  this  re 
port  in  speaking  of  the  entire  experimental 
devices  of  each  company,  rather  than  the  term 
filter  alone.  By  the  terms  of  the  contracts  be 
tween  the  Water  Company  and  the  other 
companies  the  latter  installed  their  respective 
systems,  each  having  a  capacity  of  250,000 
gallons  per  twenty-four  hours,  in  separate 
temporary  houses  at  their  own  expense.  The 
several  companies,  further,  managed  and 
operated  their  systems  without  any  expense, 
risk,  or  responsibility  to  the  Water  Company. 
Authority,  however,  was  reserved  by  the 
Water  Company  to  make  such  rules  and 
regulations  as  it  deemed  advisable  in  con 
ducting  these  tests  on  a  fair  competitive  basis, 
and  to  allow  its  representatives  unrestricted 
access  to  the  several  systems  at  all  times,  in 
order  that  such  information  could  be  obtained 
as  was  deemed  necessary  in  the  premises. 

Mr.  George  A.  Soper  was  engineer  in 
charge  of  the  Warren  Filter.  Messrs.  Will 
iam  M.  Jewell  and  Ira  H.  Jewell,  officers  of 
the  Jewell  Filter  Company,  were  in  charge  of 
the  Jewell  Filter.  Mr.  Charles  T.  Whittier 
was  chemist  in  charge  of  the  Western  Sys 
tems.  The  writer  wishes  to  express  his  ob 
ligations  to  these  gentlemen  for  their  cour 
teous  cooperation  with  him  in  conducting 
these  tests. 

The  Warren  Filter  and  the  two  Western 
Filters  were  removed  promptly  at  the  close 
of  the  competitive  tests.  Aug.  i,  1896.  The 
Jewell  Filter  and  the  Harris  Systems  were  not 
removed  at  once.  During  August,  1896,  ar 
rangements  were  made  with  the  Harris  Com 


pany  to  utilize  some  of  their  appliances  in 
supplementary  tests  made  by  the  Water  Com 
pany,  and,  when  the  investigations  were  re 
sumed  at  the  beginning  of  1897,  arrange 
ments  were  also  made  by  the  Water  Company 
whereby  these  two  experimental  plants  could 
be  used,  in  order  to  guard  against  delays. 

In  the  tests  of  electrolytical  devices  from 
Jan.  i  to  March  10,  1897,  the  professional 
services  of  Profs.  Mark  and  Brownell  were 
retained  by  the  Water  Company  to  devise 
necessary  electrical  appliances,  and  to  consult 
with  officers  of  the  Water  Company  with  re 
gard  to  their  operation.  These  new  devices 
were  installed  at  the  expense  of  the  Water 
Company  in  the  temporary  house  formerly 
occupied  by  the  Warren  Filter. 

The  settling  tank,  clay  extractor,  and  po- 
larite  filter  used  in  the  MacDougall  Polarite 
System  were  constructed  by  Mr.  MacDougall 
at  his  own  expense,  and  in  connection  with 
the  Jewell  Filter  were  operated  under  the  su 
pervision  of  Mr.  John  MacDougall. 

The  tests  of  methods  and  appliances  car 
ried  on  solely  by  the  Water  Company  were 
made  under  the  direction  of  the  Chief  En 
gineer  and  Superintendent,  Mr.  Charles  Her- 
many,  and  of  the  Chief  Chemist  and  Bacteri 
ologist.  A  large  share  of  the  engineering 
portions  of  the  work  was  done  under  the  gen 
eral  supervision  of  Mr.  Hermany,  and  the 
writer  desires  to  express  his  obligation  to  him 
for  much  valuable  advice  and  assistance  upon 
the  entire  work  obtained  in  frequent  confer 
ences  throughout  the  progress  of  the  investi 
gations.  A  large  amount  of  construction  and 
repair  work  in  the  course  of  the  tests  was  ably 
done  by  Mr.  John  Wiest,  the  engineer  in 
charge  of  the  pumping  station. 

There  was  a  considerable  difference  in  the 
amount  of  work  to  be  done  at  various  times 
throughout  the  tests,  and,  accordingly,  the 
number  of  assistants  employed  by  the  Water 
Company  varied  from  time  to  time  during 
the  two  years  of  investigation.  The  number 
ranged  from  two  to  seven,  and  averaged  a  little 
more  than  three,  exclusive  of  the  stenographer 
and  porter.  In  addition  to  the  construction 
and  repair  work  on  pipes  and  meters,  the 
Water  Company  funished  an  engineer  during 
the  competitive  tests  to  operate  the  wash- 
water  pump. 


IN  TROD  UCTJON. 


'.5 


The  following  gentlemen  were  engaged  as 
assistants  during  these  investigations,  and  to 
their  faithfulness  and  industry  a  large  share 
of  the  success  of  the  work  is  due: 

Mr.  Chas.  L.  Parmelee,  Assistant  Engineer. 

Mr.  Robert  S.  Weston,  Assistant  Chemist. 

Dr.  Hibbert  Hill,  Assistant  Bacteriologist. 

Mr.  Joseph  W.  Ellms,  Assistant  Chemist. 
•  Mr.  George  A.  Johnson,  Clerk  and  Assist 
ant  Bacteriologist. 

Mr.  Reuben  E.  Bakenhus,  Assistant. 

Mr.  Harold  C.  Stevens,  Assistant. 

All  analytical  work  connected  with  these 
investigations  was  done  in  the  laboratory  of 
the  Louisville  Water  Company,  with  the  ex 
ception  of  the  necessary  mechanical  analyses 
of  filtering  material,  which  were  made  at  the 
Lawrence  Experiment  Station  by  Mr.  Harry 
W.  Clark. 

At  the  outset  of  these  investigations  it  was 
arranged  that  bi-weekly  reports  of  progress 
should  be  made  by  the  Chief  Chemist  and 
Bacteriologist  to  the  Directors  of  the  Water 
Company,  and  to  them  alone.  Early  in  the 
competitive  tests  the  Jewell  Filter  Company 
and  the  Cumberland  Manufacturing  Com 
pany  requested  the  Water  Company  to  keep 
them  informed  as  to  the  daily  results  accom 
plished  by  their  respective  niters.  The  Water 
Company,  in  response  to  this  request,  offered 
to  furnish  the  operators  of  the  filters  tran 
scripts  of  analytical  results  obtained  from  their 
own  filters  (without  any  comments,  sum 
maries,  or  conclusions),  provided  the  filter 
companies  would  reimburse  the  Water  Com 
pany  for  the  additional  expense  incurred, 
and  that  the  transcript  of  the  results  would 
not  be  used  within  a  stated  period  for  any 
purpose  other  than  as  an  aid  to  the  intelligent 
operation  of  their  respective  filters.  The 
Jewell  Filter  Company  and  the  Cumberland 
Manufacturing  Company  accepted,  but  the 
Western  Filter  Company  declined,  this  propo 
sition.  In  compliance  therewith  the  amount 
of  analytical  work  was  increased,  beginning 
Feb.  I,  1896. 

In  order  that  the  present  report  may  be 
more  readily  understood  it  is  divided  into  six 
teen  chapters,  as  shown  below,  giving  the  full 
results  of  the  investigations  in  their  logical 
order.  With  the  exception  of  Chapter  I,  on 
the  composition  of  the  Ohio  River  water,  and 


upon  which  additional  data  were  obtained  in 
1897,  the  first  twelve  chapters  are  presented 
in  substantially  the  same  form  as  prepared  in 
1896.  It  will  be  seen  that  the  remaining 
chapters  deal  with  the  work  of  the  current 
year.  In  the  appendix  are  recorded  the 
methods  of  analyses  employed,  and  several 
other  matters  of  purely  technical  interest. 

The  chapters  into  which  the  report  is  di 
vided  are  as  follows: 

I.   Composition  of  the  Ohio  River  water. 
II.   Description     of     the     application     of 
chemicals  to  the  Ohio  River  water 
by  the  respective  systems  of  purifi 
cation. 

III.  Decomposition  and  subsequent  dispo 

sal  of  the  alum  or  sulphate  of  alu 
mina  solutions  applied  to  the  Ohio 
River  water. 

IV.  Coagulation  and  sedimentation  of  the 

Ohio  River  water  by  aluminum  hy 
drate,  formed  by  the  decomposition 
of  the  applied  alum  or  sulphate  of 
alumina. 

V.  Description  of  the  filters  through 
which  the  river  water  passed  after 
coagulation  by  aluminum  hydrate, 
and  partial  purification  by  sedimen 
tation. 

VI.  Summary  of  the  various  parts  of  the 
respective  systems,  and  a  record  of 
the  repairs,  changes,  and  delays. 
VII.  The  manner  of  operation  of  the  re 
spective  systems  of  purification,  and 
the  amount  of  attention  given  there 
to. 

VrITT.  Composition  of  the  Ohio  River  water 
after  treatment  by  the  respective 
systems  of  purification  as  shown  by 
chemical,  microscopical,  and  bac 
terial  analyses;  together  with  a 
tabulation  of  the  most  important 
data  upon  the  operation  of  the  re 
spective  systems. 

IX.  Summary  of  the  principal  data  upon 
the  efficiency  and  elements  of  cost 
of  purification,  by  the  respective 
systems,  of  the  Ohio  River  water, 
divided  into  twenty  periods,  accord 
ing  to  the  character  of  the  unpuri- 
fied  water;  together  with  a  discus- 


'4 


WATER  PURIFICATION  AT  LOUISVILLE. 


sion   of  some  of  the   more  impor 
tant  features. 

X.  Description  of  the  Harris  Magneto- 
Electric  System  of  purification,  and 
a  record  of  the  results  accomplished 
therewith. 

XI.  Description  of  the  devices  operated  by 
the  Harris  Company  in  July,  and  a 
record  of  the  results  accomplished 
therewith. 

XII.  Investigation  by  the  Water  Company 
in  August,  1896,  into  the  practi 
cability  and  economy  of  the  devices 
operated  by  the  Harris  Company. 


XIII.  Description  of  the  Mark  and  Brownell 
electrolytical  devices,  and  a  record 
of  the  results  accomplished  there 
with. 

XIV.  Description  of  the  MacDougall  Po- 
larite  System,  and  a  record  of  the 
results  accomplished  therewith. 
XV.  Description  of  the  methods  and  de 
vices  of  the  Water  Company, 
tested  during  1897,  and  a  record 
and  discussion  of  the  results  ac 
complished  therewith. 

XVI.   Final  summary  and  conclusions. 

Appendix,  containing  technical  records  of 
methods  of  analyses,  etc. 


COMPOSITION   OF  OHIO   Rll'ER    WATER. 


CHAPTER   I. 


COMPOSITION  OF  THE  OHIO  RIVER  WATER. 


THE  water  of  the  Ohio  River  at  Louisville 
varies  widely  from  time  to  time  in  its  compo 
sition.  This  variation  is  caused  by  a  number 
of  factors,  among  which  are  the  following: 

1.  The  size  and  varying  geological  forma 
tion  of  the  watershed. 

2.  The    number    of    comparatively    large 
tributaries  which  drain  areas  of  distinctly  un 
like  geological  character. 

3.  The  amount  of  precipitation  (rain  and 
snow). 

4.  The    distribution    of    the    precipitation 
over  the  watershed. 

5.  The  condition  of  the  soil  at  the  begin 
ning  of  heavy  rain-storms. 

6.  The  amount  and   rate   of   precipitation 
during  single  storms. 

7.  The  stage  of  the  river. 

8.  The  velocity  of  flow  of  the  river. 

9.  Agitation  of  the  water  in  the  river,  due 
to  wind-storms,  etc. 

The  watershed  of  the  Ohio  River  above 
Louisville  is  about  85,000  square  miles  in 
area.  This  area  includes  portions  of  the 
States  of  New  York,  Pennsylvania,  Ohio,  In 
diana,  North  Carolina,  Virginia,  West  Vir 
ginia  and  Kentucky.  Wide  extremes  in 
geological  formation  exist  in  the  watershed. 

At  Pittsburgh  the  Alleghany  and  Monon- 
gahela  rivers  unite  to  form  the  Ohio  River. 
West  of  the  city  of  Pittsburgh  the  drainage 
of  this  portion  of  the  watershed  finds  its  way 
into  the  Ohio  River  through  thirty-three 
principal  tributaries  and  a  great  number  of 
smaller  affluents.  East  of  Pittsburgh  there 
are  numerous  affluents  to  the  two  main 
streams,  but  they  are  correspondingly  small 
in  size. 

The  total  population  resident  on  this 
watershed  above  Louisville  is  estimated  at 
4,500,000,  of  which  1,575,000  is  contained  in 
220  towns  and  cities,  according  to  the  census 
of  1890,  increased  15  per  cent,  for  the  six 


years  of  the  present  decade.  The  nearest 
city  discharging  sewage  into  the  water  which 
passes  this  pumping  station  is  Madison,  In 
diana,  situated  about  50  miles  above  Louis 
ville,  with  a  population  of  about  12,000.  The 
next  city  is  Frankfort,  Kentucky,  situated  on 
the  Kentucky  River  67  miles  from  its 
mouth.  This  city,  has  a  population  of  about 
10,000.  The  Kentucky  River  joins  the  Ohio 
about  57  miles  above  Louisville.  The 
nearest  large  centre  of  population  discharg 
ing  sewage  into  this  water  supply  is  at  Cin 
cinnati,  Ohio.  Opposite  this  city  are  the 
cities  of  Newport  and  Covington,  Kentucky. 
Their  aggregate  population  (three  cities)  is 
about  420,000,  and  they  are  distant  above 
Louisville  about  150  miles  by  river. 

At  the  pumping  station  of  this  Company 
where  the  tests  and  investigations  were  con 
ducted  the  Ohio  River  is  about  1700  feet 
wide  and  20  feet  in  average  depth  at  low 
water.  At  the  Ohio  Falls,  which  are  about 
three  miles  below  the  pumping  station  and 
opposite  the  city  of  Louisville,  the  river  is 
about  4400  feet  wide  at  low  water.  When 
very  heavy  freshets  or  floods  occur  in  the 
Ohio  River  in  this  locality  they  cause  the 
river  to  overflow  its  banks  at  the  pumping 
station,  and  reach  to  the  bluffs  which  run 
parallel  to  the  river  on  the  Kentucky  side. 
The  width  of  the  river  is  then  about  5500  feet. 

The  rises  and  floods  in  the  Ohio. River, 
with  their  associated  factors,  produce  wide 
and  rapidly  changing  variations  in  the  com 
position  of  the  river  water.  Owing  to  the 
fact  that  the  composition  of  the  river  water  is 
a  prominent  factor  in  the  cost  of  purification, 
analyses  were  made  practically  every  day  dur 
ing  these  tests  of  the  water  before  its  appli 
cation  to  the  systems  of  purification.  Before 
giving  attention  to  the  results  of  analyses, 
however,  the  question  of  frequency  and  depth 
of  freshets  or  floods  is  to  be  considered. 


1 6  WATER   PURIFICATION  AT  LOUISVILLE. 

FRESHETS  OR  FLOODS  IN  THE  OHIO  RIVER.  PLAN  OF  ANALYTICAL  WORK. 


Freshets  or  floods  may  be  considered  as 
stages  or  depths  of  water  in  the  river  which 
are  above  the  normal.  Their  frequency  and 
magnitude  depend  upon  a  series  of  factors 
connected  with  the  rainfall  on  the  watershed, 
and  are  very  irregular.  By  virtue  of  the  in 
fluence  which  they  exert  indirectly  upon  the 
cost  of  purification,  and  the  method  leading 
to  the  most  efficient  and  economical  results, 
they  are  worthy  of  very  careful  consideration. 
This  is  especially  true  in  connection  with  this 
report,  because  inspection  of  the  data  pre 
sented  in  the  following  table  shows  that  during 
the  period  covered  by  the  first  portion  of 
these  tests  the  magnitude  of  freshets  or  floods 
was  below  the  normal  for  the  past  thirty-six 
years.  Practically  speaking,  this  means  that 
the  average  amount  of  mud,  silt,  and  clay  sus 
pended  in  a  given  volume  of  the  Ohio  River 
water  during  these  investigations  and  tests 
was  abnormally  small. 

In  the  following  table  is  given  a  summary  of 
the  number  and  magnitude  of  the  freshets  or 
floods  which  occurred  in  the  Ohio  River  at 
Louisville  during  the  past  thirty-six  years, 
1861  to  1896,  inclusive.  This  was  obtained 
from  curves  prepared  annually  by  the  Water 
Company  from  data  obtained  daily  at  the 
pumping  station  during  the  entire  period. 
These  annual  curves  were  made  from  plot- 
tings  of  a  convenient  scale,  in  which  the  ab 
scissae  correspond  to  the  number  of  days  in 
a  year,  and  the  ordinates  to  depths  of  water 
above  the  low-water  level.  By  connecting 
the  points  plotted  in  this  manner  curves  have 
been  obtained  which  show  the  depth  of  the 
river  water  for  each  day  of  each  year  of  this 
period.  The  number  and  extent  of  the  fresh 
ets  orjloods  were  obtained  by  noting  those 
portions  of  the  curve  corresponding  to  rising, 
fairly  stationary,  and  falling  stages  or  depths 
of  water  in  the  river.  The  end  of  a  given 
freshet  or  flood  is  shown  by  a  return  to  the 
normal  depth  of  water,  or  by  the  beginning  of 
another  freshet  or  flood  quickly  following  the 
one  in  question.  To  obtain  the  depth  of  a 
given  freshet  or  flood  from  these  curves  the 
difference  in  elevation  is  noted  between  the 
initial  and  highest  point  of  the  given  portion 
of  the  curve. 


In  the  determination  of  the  composition  of 
the  Ohio  River  water,  as  shown  by  analyses, 
attention  was  directed  to  the  physical,  chemi 
cal,  and  biological  characters  of  the  water. 

Physical  Character. — Upon  this  point  the 
examinations  included  observations  on  the  ap 
pearance  and  character  of  the  matters  in  sus 
pension,  and  on  the  odor,  color,  taste,  and 
temperature  of  the  water. 

Chemical  Character. — The  chemical  analy 
ses  included  the  determinations  of  the  total 
amount  by  weight  of  the  mineral  and  organic 
matters  dissolved  and  suspended  in  the  water; 
the  amount  of  organic  matter  in  solution  and 
in  suspension;  the  form  in  which  the  nitro 
gen  was  present  in  its  passage  through  the 
cycle  from  crude  organic  matter  (albuminoid 
ammonia)  to  completely  mineralized  matter 
(nitrates);  the  alkalinity,  due  chiefly  to  the 
carbonates  and  bicarbonates  of  calcium  and 
magnesium,  which  indicated  the  amount  of 
alum  that  could  be  effectually  decomposed  by 
the  water;  and  the  amounts  present  of  chlo 
rine,  dissolved  alumina,  iron,  and  fixed  residue 
on  evaporation  after  ignition  to  burn  up  the 
organic  matter  and  effect  incidental  changes. 
These  determinations  compose  the  regular 
sanitary  and  technical  chemical  analysis  of 
water  for  work  of  this  class. 

In  addition  to  the  regular  chemical  analy 
ses,  as  stated  above,  there  were  made  from 
time  to  time  as  occasion  presented  special 
sanitary  and  technical  analyses.  Among 
these  were  included  the  determination  of  the 
amounts  of  free  (atmospheric)  oxygen  and  car 
bonic  acid  gases,  dissolved  in  the  water;  and 
the  amounts  of  incrusting  constituents  of  the 
water  in  connection  with  its  adaptability  for 
use  in  boilers. 

Mineral  analyses  were  also  made  of  several 
samples  of  water  which  were  representative 
of  different  grades  in  the  wide  range  of  com 
position  of  the  water  met  with  in  these  inves 
tigations.  These  analyses  consisted  of  the  de 
termination  of  the  principal  metallic  elements 
and  the  acids  present  in  the  mineral  com 
pounds  contained  in  the  river  water. 

Biological  Character. — The  biological  analy 
ses  consisted  chiefly  of  the  determination  of 
the  numbers  of  bacteria  present  in  the  water, 


COMPOSITION   OF  OHIO   RIVER    WATER. 


1 8 


IVATKR   PURIFICATION  AT  LOUISVILLE. 


and  of  the  examination  of  the  species  of  bac 
teria  with  special  reference  to  their  connec 
tion  in  the  causation  of  disease. 

Microscopical  examinations  were  also  made 
from  time  to  time  to  learn  the  numbers  and 
kinds  of  alga:,  diatoms,  infusorise,  etc.,  pres 
ent  in  the  river  water.  These  microscopical 
analyses  differ  distinctly  from  the  bacterial 
analyses  in  that  the  former  relate  solely  to 
those  relatively  large  micro-organisms  which 
may  be  counted  and  classified  with  the  aid  of 
comparatively  low  powers  of  the  microscope; 
while  the  bacteria  are  so  small  (about  o.oooi 
inch  in  length)  that  they  require  for  their 
enumeration  and  classification  special  meth 
ods  of  laboratory  procedure. 

Preceding  the  several  tables  showing  the 
results  of  analyses  there  will  be  found  ex 
planatory  notes,  calling  attention  to  the  na 
ture  of  the  principal  points  of  practical 
significance.  At  the  close  of  the  report  is  an 
appendix  in  which  is  presented  a  record  of 
some  of  the  more  important  features  of  the 
analytical  methods  from  a  technical  stand 
point. 

The  plan  of  analytical  work,  which  has 
been  briefly  outlined  in  the  foregoing  para 
graphs,  may  be  made  plainer  by  the  following 
synopsis: 

Synopsis  of  Analytical  Work. 

1.  Physical:  Appearance,   odor,   color,   taste, 

and  temperature. 

2.  Chemical:  Regular  sanitary  and  technical 

analyses. 
Special  sanitary  and  technical 

analyses. 
Mineral  analyses. 

3.  Biological:  Microscopical  examinations. 

Quantitative  bacterial  analyses. 

Identification  of  species  of  bac 
teria,  with  special  reference 
to  the  causation  of  disease. 

Place  of  Collection  of  Samples  of  River  Water 
for  Analysis. 

Samples  of  river  water  for  analysis  were 
collected  from  a  tap  on  a  6-inch  pipe.  This 
tap  was  kept  open  during  working  hours. 
The  6-inch  pipe  was  about  230  feet  in  length, 


and  connected  with  the  force  main  leading  to 
the  distributing  reservoir  at  Crescent  Hill. 
From  the  intake  to  the  point  where  the  6-inch 
pipe  branched  from  the  force  main  the  dis 
tance  was  about  390  feet.  In  this  distance 
the  water  passed  through  the  pump  well  and 
the  pump  which  was  operated  to  supply  the 
city. 

The  intake  of  the  water  supply  is  located 
3.5  feet  below  the  low-water  stage  and  about 
100  feet  from  the  Kentucky  shore  at  low 
water. 

Manner   of    Collection    of    Samples    of   River 
Water  for  Analysis. 

After  the  investigations  were  well  under 
way  it  was  the  general  custom  to  collect  on 
each  working  day,  from  the  above-described 
place,  one  sample  of  water  for  regular  chemi 
cal  analysis,  and  two  or  more  samples  for  the 
determination  of  the  numbers  of  bacteria. 
When  the  systems  of  purification  were  in  op 
eration  night  and  day  samples  of  water  for 
both  chemical  and  bacterial  analyses  were  col 
lected  once  in  six  hours.  In  the  case  of  the 
chemical  samples  four  portions  were  mixed 
together  to  give  a  representative  sample  for 
the  day. 

Samples  of  water  for  other  analytical  pur 
poses  were  collected  from  time  to  time  as 
occasion  demanded,  and  as  the  pressure  of 
regular  work  allowed  of  their  analysis. 

All  samples  were  placed  in  a  large  ice-box 
during  the  period  which  intervened  between 
their  collection  and  their  analysis. 

PHYSICAL  CHARACTER  OF  THE  OHIO  RIVER 
WATER. 

The  most  noticeable  of  the  physical  charac 
ters  of  the  Ohio  River  water  is  its  appearance 
with  regard  to  the  matters  suspended  in  it. 
At  no  time  was  the  river  water  clear  and  free 
from  suspended  matters.  During  October 
and  the  greater  part  of  November,  1895,  the 
water  was  comparatively  clear;  but  even  at 
that  time  it  had  a  distinct  turbidity  due  to 
the  presence  of  minutely  divided  particles. 
The  first  heavy  rains  caused  the  water  to  be 
come  muddy.  From  that  time  until  the  close 
of  the  investigations  the  appearance  of  the 


COMPOSITION  OF  OHIO  RIVER  WATER. 


river  water  possessed  a  wide  range  of  rapidly 
changing  variability. 

As  a  means  of  expression  of  the  relative  ap 
pearance  of  the  Ohio  River  water  the  use  of 
adjectives  fails  utterly.  The  best  idea  of  the 
varying  appearance  of  the  water  is  obtained 
from  the  results  of  the  daily  determination 
of  the  weight  of  the  matter  suspended  in  it. 
These  results  form  a  portion  of  the  regular 
chemical  analyses;  and  reference  is  made  to 
the  following  tables  in  which  they  are  pre 
sented,  and  to  an  explanation  of  them  in  the 
note  which  precedes  the  tables.  Here  it  will 
suffice  to  state  that  the  weight  of  organic  and 
mineral  matter  suspended  in  the  water  ranged 
from  i  to  5,311  parts  per  million.  The  ratio 
between  the  weights  of  the  maximum  and 
minimum  suspended  matter,  therefore,  was 
5,311  to  i. 

The  appearance  of  the  suspended  matter  it 
self  was  quite  different  from  time  to  time, 
ranging  from  a  light  gray  to  a  dark  red  color. 
•  A  series  of  factors  influenced  the  appearance 
in  this  regard.  Prominent  among  them  was 
the  character  of  the  soil  on  which  the  rain  fell. 
The  extreme  conditions  of  muddy  water  in 
connection  with  the  appearance  of  the  sus 
pended  matter  were  noted  in  March  and  in 
May,  1896.  During  March  heavy  rains  fell 
throughout  the  valley.  All  the  tributaries 
were  in  flood,  and  during  the  last  days  of 
the  month,  when  the  velocity  of  the  Ohio 
River  was  great,  the  water  had  a  decided 
red  appearance.  These  particles  were 
comparatively  large  and  came,  apparently, 
from  the  upper  portion  of  the  water 
shed. 

In  April  and  May,  1896,  there  was  a  period 
of  extended  drought  and  the  surface  of  the 
earth  was  very  dry.  The  rains  which  came 
during  the  last  week  in  May  produced  muddy 
water,  which  contained  an  immense  number 
of  minutely  divided  particles  of  a  light  gray 
color.  This  gave  the  water  a  yellowish  ap 
pearance.  Some  of  the  particles  were  smaller 
than  bacteria  and  measured  under  the  micro 
scope  less  than  o.ooooi  inch  in  diameter. 
Naturally  enough  this  water  was  very  difficult 
to  clarify. 

Between  these  extreme  conditions  of  ap 
pearance  there  was  a  wide  range  of  intermedi 
ate  conditions,  depending  upon  the  relative 


influence  of  the  series  of  factors  outlined  on 
page  15. 

During  1897  there  was  a  still  greater  range 
than  during  1895-96  in  the  amounts  and 
character  of  the  suspended  matter  in  the  river 
water,  although  at  no  time  were  the  clay  par 
ticles  finer  than  in  May,  1896.  Further,  it 
appears  that  the  heavy  mud  is  most  prevalent 
during  the  winter  and  early  spring,  while  the 
fine  clay  prevails  in  the  late  spring  and 
summer. 

Odor  of  the  River  Water. 

The  Ohio  River  water,  when  it  was  not 
heated,  possessed  as  a  rule  a  faint  odor,  the 
intensity  of  which  was  somewhat  variable. 
Occasionally  the  odor  was  quite  pronounced, 
but  often  no  odor  could  be  detected.  Dur 
ing  the  fall,  winter,  and  early  spring  the  odor 
was  usually  musty,  sometimes  aromatic  and 
resinous.  After  the  rains  in  the  spring  the 
odor  had  a  vegetable  character  at  times. 

Upon  heating  the  river  water  the  odor  be 
came  stronger,  especially  in  the  case  of  the 
vegetable  odor  noticed  during  warmer 
weather. 

In  practically  no  case,  however,  was  the 
odor  disagreeable,  or  stronger  than  would  be 
expected  in  a  surface  water  of  this  kind. 

Color  of  the  River  Water. 

It  is  the  suspended  particles  in  the  river 
water  which  give  to  it  a  color.  This  has  al 
ready  been  referred  to  under  the  appearance 
of  the  water. 

When  the  water  is  freed  from  its  suspended 
particles  it  is  practically  colorless. 

In  the  following  tables  containing  the  re 
sults  of  the  regular  chemical  analyses  will  be 
found  a  record  of  the  amount  of  dissolved 
color,  expressed  in  units  of  the  platinum- 
cobalt  standard.  These  color  results  were 
obtained  after  the  suspended  particles  had 
been  removed  by  the  passage  of  the  water 
through  a  fine  paper  filter  or  a  Pasteur  filter. 

Taste  of  the  Rh'cr  Water. 

Disregarding  the  suspended  matter,  the 
taste  of  the  river  water  is  satisfactory,  al- 


WATER   PURIFICATION  AT  LOUISVILLE. 


though  the  salts  dissolved  in  it,  especially  the 
lime,  give  a  slight  taste  which  is  noticed  by 
those  accustomed  to  drinking  a  softer  water. 
There  is  at  times  a  slight  earthy  taste  to  the 
water. 

The  suspended  matter  cannot  be  regarded 
as  other  than  objectionable.  But  after  per 
sons  become  familiar  with  this  kind  of  water 
there  appear  to  be  comparatively  few  com 
plaints,  except  when  the  water  is  very  muddy. 

Temperature  of  the  River  Water. 

The  results  of  observations  on  the  tem 
perature  of  the  river  water,  expressed  in  de 
grees  centigrade,  are  presented  in  the 
tables  beyond,  containing  the  results  of  the 
regular  chemical  analyses. 

CIIFMICAL  CHARACTER  OF  THE  OHIO  RIVER 
WATER. 

In  the  next  set  of  tables  there  are  pre 
sented  the  results  of  the  regular  chemical 
analyses  of  the  river  water  from  a  sanitary 
and  technical  standpoint. 

The  times  of  collection,  the  temperature, 
and  the  color  results  will  be  readily  under 
stood  from  the  foregoing  pages.  They  are 
recorded  here  as  a  matter  of  convenience. 

The  remaining  columns  contain  the  resul  s 
of  the  several  chemical  determinations.  An 
outline  of  the  analytical  methods  used  in  these 
chemical  determinations  will  be  found  in  the 
appendix.  In  order  that  the  practical  signifi 
cance  of  these  results  may  be  understood  more 
clearly  a  brief  explanation  of  them  will  be 
given. 

Explanation  of  the  Results  of  Chemical 
Analyses. 

The  several  points  will  be  taken  up  in  the 
order  in  which  they  appear  in  the  tables. 

Form  of  Expression. — All  of  these  results 
are  expressed  in  parts  per  million.  The  exact 
meaning  of  this  is  that  one  million  parts  of 
water  by  volume  contained  the  several  sub 
stances  in  parts  by  weight  to  the  extent  in 
dicated  by  the  figures. 

These  results  may  be  converted  into  grains 


per  United  States  gallon  (231  cubic  inches) 
by  dividing  by  17.1. 

Oxygen  Consumed. — The  results  of  this  de 
termination  indicate  the  amount  of  organic 
matter  present  in  the  water.  By  analytical 
methods  there  is  measured  the  amount  of  oxy 
gen  which  is  actually  consumed  by  the  or 
ganic  matter  in  the  water,  as  it  is  converted 
into  a  comparatively  stable  form  not  readily 
capable  of  farther  decomposition  by  ordinary 
means. 

As  nitrogen  cannot  be  oxidized  by  this 
method  these  results  are  generally  considered 
to  be  indicative  of  the  amount  of  organic 
matter  of  a  carbonaceous  nature. 

Nitrogen  as  Albuminoid  Ammonia. — When 
water  containing  organic  matter  of  a  nitrog 
enous  nature  is  distilled  with  a  strong  alka 
line  solution  of  potassium  permanganate,  the 
organic  nitrogen  is  changed  to  ammonia. 
This  ammonia  is  spoken  of  as  "  albuminoid 
ammonia,"  and  the  results  of  determinations 
by  this  method  indicate  the  amount  of  or 
ganic  matter  of  a  nitrogenous  nature. 

A  comparison  of  the  results  of  analyses  by 
the  last  two  methods  indicates  that  the  nature 
of  the  organic  matter  in  the  river  water  varied 
considerably,  according  to  the  relative  results 
by  these  methods  for  its  determination. 

It  will  also  be  noted  in  the  tables  that  the 
results  by  the  second  method  show  the 
amounts  of  organic  matter  in  suspension  and 
in  solution,  respectively.  Comparatively 
speaking,  the  amount  of  nitrogenous  organic 
matter  in  solution  is  fairly  constant,  although 
it  varied  somewhat  at  different  seasons  of  the 
year. 

Nitrogen  as  Free  Ammonia. — Upon  the  dis 
tillation  of  the  river  water  without  chemicals 
there  is  obtained  in  the  distillate  a  small  quan 
tity  of  ammonia.  This  is  known  as  the 
"  nitrogen  in  the  form  of  free  ammonia."  It 
measures  the  amount  of  nitrogenous  organic 
matter  which  has  undergone  the  initial  step  in 
the  decomposition  of  organic  matter  by  na 
ture. 

This  decomposition  in  nature  is  accom 
plished  in  the  presence  of  oxygen  by  bacteria 
which  eventually  convert  crude  organic  mat 
ter  into  harmless  mineral  matter. 

Nitrogen  as  Nitrites. — These  results  show 
the  amount  of  organic  matter  that  is  in  the 


COMPOSITION  OF  OHIO  RIVER 


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WATER  PURIFICATION  AT  LOUISVILLE. 


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WATER   PURIFICATION  AT  LOUISVILLE. 


second  intermediate  stage  of  the  process  in 
nature  by  which  organic  matter  is  converted 
to  mineral  matter. 

Nitrogen  as  Nitrates. — From  these  results 
there  is  learned  the  amount  of  organic  matter 
which  has  been  completely  oxidized  and 
changed  into  the  form  of  mineral  matter. 

Chlorine. — Chlorine  is  usually  supposed  to 
be  present  in  water  as  common  salt  for  the 
most  part.  Some  of  it  very  likely  comes  from 
mineral  deposits  on  this  watershed.  Salt  is 
also  present  in  sewage,  and  this  is  one  of  the 
reasons  why  it  is  accurately  determined. 

The  determination  of  chlorine  is  also  of 
value  in  studying  the  composition  of  a  water 
by  virtue  of  the  fact  that  it  is  not  affected  by 
any  ordinary  conditions  which  waters  meet  in 
nature.  It  is  always  soluble,  and  cannot  be 
oxidized  or  reduced.  For  this  reason  it  does 
not  pass  through  a  cycle  of  changes  as  does 
nitrogen.  A  comparison  of  the  nitrogen  and 
chlorine  is  therefore  instructive. 

Residue  on  Evaporation. — The  residue  on 
evaporation  shows  the  total  weight  of  the 
solid  matter  which  the  water  contained.  In 
the  following  tables  the  total  residue  is  sub 
divided  into  suspended  and  dissolved  residues 

Attention  is  especially  called  to  the  sus 
pended  residue  on  evaporation.  This  shows 
the  weight  of  the  matters  suspended  in  the 
water,  and  gives  a  good  general  idea  of  what 
the  relative  appearance  of  the  water  was  on 
the  different  days. 

Fixed  Residue  after  Ignition. — After  weigh 
ing  the  total  residue  of  the  water  upon  evapo 
ration  it  is  the  custom  to  heat  the  platinum 
dish  containing  the  residue  to  a  dull  red  point 
and  again  weigh  it.  By  this  means  the  fixed 
residue  is  obtained. 

Formerly  it  was  supposed  that  this  ignition 
burnt  off  the  organic  matter,  and  the  differ 
ence  in  weight  of  the  contents  of  the  dish 
would  give  the  amount  of  organic  matter 
present  in  the  water.  This  is  not  true,  how 
ever,  because  the  ignition  volatilizes  certain 
mineral  constituents  of  the  water,  which  would 
be  erroneously  figured  as  organic  matter. 

Nevertheless,  the  fixed  residue  on  evapora 
tion  appeared  to  be  of  some  value  in  studying 
the  comparative  composition  of  the  mineral 
constituents  of  the  water. 

Alkalinity. — This   determination  is  one  of 


great  importance  in  connection  with  the  puri 
fication  of  water  by  the  method  under  investi 
gation.  These  results  show  the  amount  of 
carbonates  and  bicarbonates  of  calcium  and 
magnesium  which  were  present  in  the  water. 
It  is  these  compounds  which  decompose  alum 
or  sulphate  of  aluminum,  as  is  explained  in 
Chapter  III. 

The  results  are  expressed  in  terms  of  cal 
cium  carbonate  (lime).  They  are  somewhat 
similar  to  the  "  temporary  hardness  "  deter 
mination  by  the  "  soap  method." 

Dissolved  Alumina.  —  No  appreciable 
amount  of  dissolved  alumina  could  be  found 
in  the  river  water.  The  results  of  the  tests 
are  recorded,  however,  as  they  are  of  value 
in  the  study  of  the  question  as  to  the  passage 
of  alum  through  the  systems  into  the  filtered 
water. 

Iron. — The  results  of  the  determination  of 
iron  are  of  value  in  showing  variations  in  the 
composition  of  the  suspended  matter  in  the 
water.  Practically  all  of  the  iron  was  con 
tained  in  the  suspended  matters. 


Special  Chemical  Analyses. 

There  were  several  sanitary  and  technical 
problems  under  consideration,  which  re 
quired  special  chemical  analyses  from  time 
(o  time,  as  follows: 

1.  Atmospheric   oxygen    dissolved    in   the 
water. 

2.  Carbonic  acid  gas  (carbon  dioxide)  dis 
solved  in  the  water. 

3.  Those  dissolved  chemicals  in  the  water 
which  give  to  the  water  its  "  permanent  hard 
ness  "  and  its  power  to  produce  incrustations 
in  steam-boilers. 

The  first  set  of  these  data  was  fairly  com 
plete,  from  a  practical  point  of  view,  during 
1895-96,  and  the  analyses  were  made  less  fre 
quently  in  1897.  With  regard  to  the  latter 
sets  of  data,  however,  the  evidence  early  in 
1897  showed  that  these  constituents  were  so 
variable  and  of  such  importance  that  they 
were  included  in  the  regular  analyses.  As  a 
matter  of  convenience,  however,  the  results 
are  recorded  here;  but  reference  to  the  fore 
going  tables  will  show  their  relation  to  other 
constituents  of  the  water.  The  significance 


COMPOSITION  OF  OHIO   RIVER    WATER. 


33 


of  these  results  is  explained  and  discussed  in 
subsequent  chapters. 

Dissolved  Oxygen  in  the  River  Water. — 
These  results  are  of  value  in  connection  with 
the  preservation  of  the  quality  of  the  water 
after  purification,  and  for  a  comparison  of  the 
water  before  and  after  treatment,  especially 
in  the  electrolytic  process  with  iron  elec 
trodes.  The  amount  of  atmospheric  oxygen 
which  may  be  contained  in  the  river  water  is 
limited  by  the  saturation  of  oxygen  gas  in  the 
water;  and  the  saturation  depends  chiefly  on 
the  temperature  (and  pressure),  the  amount 
of  oxygen  necessary  for  saturation  decreasing 
as  the  temperature  increases.  In  the  adjoin 
ing  table  the  amounts  of  oxygen  gas  dis 
solved  in  the  river  water  are  expressed  in 
parts  by  weight  per  million  parts  of  water  by 
volume,  and  in  percentages  of  the  amounts 
necessary  for  the  saturation  of  the  water  at 
the  actual  temperature  at  the  time  of  col 
lection. 

Carbonic  Acid  Gas  Dissolved  in  the  River 
Water. — As  an  aid  in  an  investigation  into 
the  influence  of  carbonic  acid  gas  (carbon  di 
oxide)  upon  the  corrosive  action  of  the  river 
water  before  and  after  purification  by  differ 
ent  methods,  the  amount  of  this  gas  which 
was  naturally  dissolved  in  (he  river  water  with 
the  formation  of  carbonic  acid  was  deter 
mined  with  results  given  on  page  34.  It  de 
veloped  in  the  course  of  the  tests  that  the 
determinations  of  carbonic  acid  gas  are  of 
more  importance  than  was  generally  sup 
posed  to  be  the  case  formerly,  and.  as  stated 
above,  the  analyses  were  made  with  more  fre 
quency  in  1897  than  during  the  first  part  of 
the  work.  In  passing  it  may  be  noted  that 
at  times  the  weight  of  carbonic  acid  gas  dis 
solved  in  the  river  water  equalled  and  even 
exceeded  the  weight  of  all  solid  matters  dis 
solved  in  the  water. 

Hardness  of  the  River  Water. — The  hard 
ness  of  a  water  depends  upon  the  presence  of 
dissolved  salts  of  calcium  (lime)  and  magne 
sium.  These  salts  consist  of  the  carbonates, 
bicarbonates,  sulphates,  chlorides,  and  ni 
trates.  The  bicarbonates  are  carbonates 
which  are  held  in  solution  by  carbonic  acid. 
For  many  years  it  has  been  the  custom  to 
subdivide  hardness  into  "  temporary  hard 
ness  "  and  "  permanent  hardness."  Tempo- 


PARTS  PER  MILLION  OF  ATMOSPHERIC  OXY 
GEN  DISSOLVED  IN  THE  OHIO  RIVER 
WATER,  WITH  PERCENTAGES  SHOWING 
THE  RELATION  BETWEEN  THE  AMOUNTS 
FOUND  AND  THOSE  NECESSARY  FOR  SAT 
URATION  AT  ACTUAL  TEMPERATURES. 


Date. 

181,5. 

Tempera- 

Dissolved  Atmospheric  Oxygen. 

Parts  per  Million. 

Percentages  which  the 

of  the  Amounts 
Required  for 
Saturation. 

Satura- 

Found. 

Dec.    3 

3-4 

2.32 

10.3 

78 

"       4 

4-5 

2-57 

9-5 

76 

"       6 

4-2 

2.69 

0.2 

80 

"       9 

4.1 

2.88 

1.2      . 

87 

1896 

Jan.  II 

2.1 

3.52 

1.6 

86 

Feb.  10 

5-9 

2.19 

1-3 

93 

"      15 

7-0 

1.90 

1.6 

97 

"     26 

3-4 

3.01 

3-° 

IOO 

Mar.    4 

4.4 

2.61 

1.6 

92 

"      II 

6.5 

2.01 

0.8 

90 

"      19 

5-2 

2.38 

2-4 

IOO 

Apr.  9 

9.9 

1.16 

O.  2 

91 

May    6 

23.1 

8.47 

7-2 

85 

"     '4 

24.0 

8.34 

6.6 

79 

"     23 

24.5 

8.28 

6.2 

75 

"     29 

24.7 

8.25 

5-9 

71 

June    5 

24.2 

8.32 

6-3 

76 

"       10 

24-7 

8.25 

66 

So 

"     18 

25-3 

8.20 

6.4 

78 

"     24 

26.8 

8.02 

6.4 

80 

July    9 

25-5 

8.17 

5-9 

72 

"     18 

25.6 

8.15 

5-8 

7i 

1897 

April  10 

«-3 

10.81 

10.  1 

93 

"      20 

it.  6 

10.75 

10.  I 

94 

"     29 

16.3 

9.61 

8.5 

88 

June    4 

20.9 

8.81 

8.7 

99 

"       5 

21.8 

8.65 

8-7 

IOO 

"     17 

26.7 

8.04 

7-4 

92 

"     18 

29.1 

7-73 

6.6 

85 

"     25 

26.0 

8.  II 

6-7 

82 

"     27 

25  3 

8.20 

6.9 

84 

11     28 

25-3 

8.20 

6.6 

81 

"     3° 

26.2 

8.09 

8.0 

99 

July    1 

26.6 

8.05 

6.7 

83 

1       3 

27.6 

7-95 

6.2 

78 

1      9 

30.0 

7.76 

5-4 

69 

'     '3 

26.5 

8.05 

6.8 

84 

'4 

27.2 

7.98 

7.0 

88 

'       10 

26.  i 

8.10 

8.0 

99 

'       20 

26.8 

8.02 

8.0 

IOO 

"       21 

27-5 

7.96 

8.0 

IOO 

"       23 

27.7 

7-94 

6.5 

82 

"     27 

26.2 

8.09 

4-6 

57 

rary  hardness  is  caused  by  bicarbonates  of 
lime  and  magnesia  which  are  precipitated 
upon  boiling,  due  to  the  expulsion  of  car 
bonic  acid  gas.  The  remaining  salts  of  lime 
and  magnesia,  as  stated  above,  have  been  re 
garded  as  permanent  hardness. 

The  practical  significance  of  the  above- 
stated  salts  of  lime  and  magnesia  is  twofold 
in  connection  with  these  investigations, 
namely: 


34 


WATER   PURIFICATION  AT  LOUISVILLE. 


AMOUNT  OF  CARBONIC  ACID  GAS  (CARBON 
DIOXIDE)  DISSOLVED  IN  THE  OHIO  RIVER 
WATER. 

(Parts  per  Million.) 


Date. 

1896. 

Car- 
Acid 
Gas. 

Date. 
1897. 

Car- 
Acid 
Gas. 

Date. 

,897. 

bonic 
Acid 

June  18 

30.8* 

April    3 

53-5 

May  29 

IOI.6 

"      22 

26.4* 

"       7 

79.6 

June     I 

66.6 

"     24 

27.7* 

"       8 

46.0 

2 

90.5 

"     27 

29.7* 

"       9 

gi.o 

'      4 

82.7 

July  3 

30.6* 

"       10 

So.o 

7 

89.0 

"       8 

21.  I* 

"      12 

65.0 

"     10 

133.0 

Nov.  28 

83.0 

"       13 

44.0 

"     it 

107.6 

Dec.  10 

98.0 

"       14 

75-7 

"    15 

98.8 

1897 

"     15 

88.3 

"     16 

103.3 

Feb.  16 

80.4 

"     16 

50.2 

"     17 

107.6 

Mar.   2 

63.4 

"      21 

41.2 

"     18 

82.7 

"       3 

59.0 

'      22 

42.7 

"     19 

106.3 

'      4 

67.8 

'      23 

43-0 

"     20 

100.3 

"       5 

49-3 

'      25 

55  o 

'      21 

100.3 

11       6 

47-6 

'      27 

94-9 

'      22 

100.3 

'       7 

51-4 

'      29 

85-9 

'      23 

107.4 

'     II 

99-5 

May    4 

S6.S 

'      24 

100.3 

'      12 

S8.o 

7 

57-4 

'     25 

105.6 

'      13 

122.4 

"       8 

1  10.6 

'   26 

"3-7 

'     15 

45-8 

"       9 

66.  7 

"   27 

I2O.O 

'     16 

33-4 

"     10 

72.1 

"   28 

92.1 

'     19 

38.8 

"     13 

65.2 

"   30 

105.9 

'     20 

42.6 

"     !4 

76.6 

July    i 

93-9 

'      22 

46.4 

"    15 

50.8 

:         2 

75-3 

'      23 

40.4 

"     IS 

67.3 

'       3 

73.1 

'      24 

44-9 

"     19 

71.8 

'       6 

100.4 

'      25 

41.9 

"      21 

88.7 

'       7 

106.  j 

'      26 

36.5 

"      22 

95-9 

'       8 

99.9 

'      27 

47.0 

"      23 

94-3 

'      12 

71.  S 

"      29 

56.6 

"      26 

So.  2 

'       15 

47.0 

"      30 

So.o 

"      27 

So.o 

'     16 

28.  S 

Apiil    t 

53-6 

"      28 

107.3 

'     17 

49-4 

*  The  results  of  June  and  July.  1896,  were  obtained 
by  the  Pettenkoffer  method,  without  the  Trillich  modi 
fication,  and  are  probably  much  too  low. 

1.  It  is  the  carbonates  and  bicarbonates  of 
lime  and  magnesia  in  the  river  water  which 
possess  the  power  of  decomposing  such  ap 
plied  chemical  products  as  alum  and  sulphate 
of  alumina,  and  thereby  forming  the  gelati 
nous  hydrate  of  aluminum  that  acts  as  a  co 
agulant. 

2.  It    is    the    remaining    salts    (sulphates, 
chlorides,  and  nitrates)  of  lime  and  magnesia 
which  are  connected  with  the  formation  of  in 
crustations  when  the  water  is  used  in  steam- 
boilers. 

By  the  old  Clark  method  of  getting  the  bi- 
.  carbonates,  called  temporary  hardness,  the 
full  power  of  the  water  to  decompose  the 
commercial  chemicals  stated  above  is  not  re 
corded,  because  it  does  not  include  the  car 
bonates.  In  practice  it  is  found  that  the  car 


bonates  will  decompose  3  grains  or  more  of 
sulphate  of  alumina  per  gallon.  To  use  a 
method  which  shows  only  the  bicarbonates  is, 
therefore,  inadmissible;  and  Hehner's  method 
was  employed.  This  method  furnished  what 
is  required,  that  is,  both  the  carbonates  and 
bicarbonates.  For  the  sake  of  explicitness 
these  results  are  recorded  as  the  alkalinity  of 
the  water  in  the  foregoing  tables  of  analyses. 
As  the  Ohio  River  possesses  no  carbonate 
or  bicarbonate  of  soda  or  potash,  the  full 
alkalinity  of  the  water  is  due  to  the  carbon 
ates  and  bicarbonates  of  lime  and  magnesia. 

By  the  old  Clark  method  the  carbonates  of 
lime  and  magnesia  are  recorded  with  the  "  in- 
crusting  constituents  "  or  "  permanent  hard 
ness."  The  facts  show  that  these  two  com 
pounds  are  permanent,  but  they  form  a 
sludge,  and  not  an  incrustation,  in  steam-boil 
ers.  By  the  Hehner  method,  which  was  em 
ployed  in  these  investigations,  the  carbonates 
are  not  included  in  the  following  table  of  re 
sults,  which,  in  the  absence  of  a  better  name, 
are  termed  the  "  incrusting  constituents  "  of 
the  water.  These  results,  which  are  dis 
cussed  in  Chapter  XV,  are  expressed  accord 
ing  to  the  conventional  method  in  equivalent 
parts  of  calcium  carbonate.  A  further  con 
sideration  of  the  methods  of  analyses  will  be 
found  in  the  appendix. 

The  dissolved  salts  of  lime  and  magnesia 
are  a'so  of  importance  in  connection  with  the 
consumption  of  soap  when  the  water  is  used 
for  washing  purposes.  This  point  is  practi 
cally  uninfluenced  by  the  purification  pro 
cesses  under  consideration,  but  the  range  of 
variation  in  this  soap-consuming  ingredient 
may  be  noted  by  taking  the  sum  of  the  alka 
linity  and  incrusting  ingredients.  See  first 
table  on  page  35.  These  results  approximate 
the  total  hardness  results  obtained  by  the 
Clark  method. 


Mineral  Analyses  of  the  Ohio  River  Water. 

A  record  of  the  results  of  the  determination 
of  the  mineral  constituents  of  the  river  water 
is  presented  in  the  next  table.  Eight  samples 
were  analyzed  with  as  much  completeness  as 
circumstances  allowed;  and  the  results  show 
very  clearly  the  marked  variations  which  the 


COMPOSITION  OF  OHIO   RIVER    WATER. 


INCRUSTING     CONSTITUENTS     OF     THE    OHIO 

RIVER   WATER. 

(Parts  per   Million.) 

Incrust- 

Incrust- 

Incrust- 

Date. 

ing 

D;ite. 

ing 

Date 

mg 

1895. 

Constit 

1897. 

,897. 

Constit 

uents. 

UelHS. 

uents. 

Dec.  9-1  1 

43-9 

Mar.  25 

10.0 

May  19-20 

IO.S 

1896 

"     26 

13-9 

21 

II.9 

May    6 

43-0 

"     29 

12.8 

"     21-23 

15.9 

'     M 

33-8 

"     30 

33-3 

"     23-24 

IO.  2 

"       22 

40.1 

Apr.         I 

29.1 

25J       20.2 

"       2g 

41.1 

"       2-3 

18.2 

"      25-26,       14.5 

June  ii 

44.0 

3-4 

II.  0 

27      16.7 

•'     18 

30.0 

5 

29.9 

"      27-28]       19.3 

July  30 

35-0 

6 

23.4 

"     28-29      16.8 

1897 

"       6-7 

30.0 

31    I  I7  n 

Feb.  17 

18.7          "            8 

19.8 

June         i    f1?'0 

"  .  22 

24.7          "           9 

14.2 

2-3       17-6 

"     23 

17.2   i      "9-0 

13  3 

4-5!     23.5 

"   24 

21.2     j                      I 

9.0 

7-8      22.5 

"     25 

It,   I 

2 

12.7 

9-10.     23.8 

"   26 

10.  0 

"  13-  4 

If).0 

11-12'     28.8 

"   27 

S.o 

'  M-  5 

2O.O 

21        28.8 

Mar.     I 

15.8 

'  15-  6 

iS.i 

22        3I.O 

2 

10.0 

'  20-21 

15-5 

23        31-8 

'       3 

8.0 

'  21-22 

17.5 

24        27.8 

4 

12.  0 

22 

12.  0 

25 

21.9 

'       5 

25-3 

'   22-23 

14.6 

27 

19.0 

•       (, 

34-6 

'   23-24 

U.3 

28 

17-5 

'       7 

1  6.0 

27 

12.7 

29-30 

25-5 

'       9 

23.4 

28 

17.0 

July          2 

20.  0 

"     10 

17.9 

29 

32.0 

6 

20.9 

"     n 

30.0 

"  29-30 

21-7 

7 

47.0 

"      12 

'      '5 

33-u 
14.0 

30 

May        I 

f-  20.0 

9-10 
'     12-13 

II.  O 

12.8 

'     16 

20.5 

4 

23.0              '      14-15         14.8 

'     17 

24.6 

5 

17.0                       l6j      14.0 

'     18 

36.0 

"       6-7 

15.5            '     17-18       12.3 

'     19 

16.7 

8-y 

15.8          "     19-20      24.2 

'      20 

22.0 

13 

I6.I            "      21-22        24.2 

'      22 

12.4 

14 

23.2            "      23-24       43.8 

'      23 

9.0 

15 

"•3 

'      24 

10.8 

"  17-19 

9.0 

composition  of  the  river  water  possessed  dur 
ing  these  investigations.  I 


The  sample  which  was  collected  on  May  29 
and  30,  1896,  was  analyzed  both  before  and 
after  nitration  through  fine  filter-paper.  At 
this  time  the  water  contained  a  large  amount 
of  very  finely  divided  particles;  and  it  was 
probably  the  most  difficult  water  to  purify 
without  subsidence  that  was  encountered  dur 
ing  the  whole  work.  The  sample  was  col 
lected  just  after  a  heavy  rain,  following  an 
extended  period  of  drought. 

From  March  23  to  29,  inclusive,  the  sam 
ple  for  analysis  was  prepared  by  mixing  equal 
small  portions  of  the  river  water  collected 
every  six  hours.  During  this  time  the  sys 
tems  of  purification  were  in  operation  night 
and  day.  By  automatic  devices  samples  of 
filtered  water  were  collected,  representing  the 
entire  period.  The  analyses  of  the  filtered 
water  are  presented  in  Chapter  VII. 

According  to  the  general  custom  the  re 
sults  of  the  determination  of  the  various  ele 
ments  in  the  water,  both  metallic  and  acid, 
are  expressed  in  the  following  table  of 
analyses  in  the  form  of  oxides  (except  the 
chlorine). 

As  would  naturally  be  expected  in  the 
water  of  a  river,  the  watershed  of  which  offers 
such  a  wide  range  in  the  possibilities  for  dif 
ferent  kinds  of  rock  disintegration  and  sur 
face  erosion,  the  relative  amounts  of  the 
mineral  constituents  are  seen  to  vary  widely. 
This  is  shown  very  forcibly  in  the  following 
table,  in  the  case  of  suspended  matters,  by  a 
comparison  of  the  ratio  existing  between  the 
alumina  and  the  oxide  of  iron. 


RESULTS    OF    MINERAL    ANALYSES   OF    THE   OHIO    RIVER   WATER. 
(Parts  per  Million.) 


Periods  of  Collection. 

,895 

,896 

Oct.  28 
No'v°  M. 

NOV.  23 

Nov.  29. 

Dec.  9 
Dec.  20. 

Jan",, 

Feb.  7 
Feb.  27. 

Feb.  28 
Mar.  18. 

Mar.  23 
Mar.  29. 

May  29  and  30. 

Unfil- 
tered. 

Filtered. 

Silica  (SiO,)        

II  .2 

0.2 

3-7 

25.9 
0.4 

3-9 
[o, 

58.2 

28.4 
3-7 
7-3 
1.4 

49.0 
13.8 

227.2 
21  .6 
15-7 
0,) 

39.6 

206.7 
26.0 
70.0 

42   f) 
6.4 
5-9 

299.5 
39-4 
76.6 
2.2 
I  .  I 
31   7 
14.0 
8.5 
18.1 

325-3 
32.8 
131.4 
3-4 

2-9 

69.2 

28.1 

93 
0.6 

0 

o 
Trace. 

47-7 
3-9 

Oxide  of  iron  (FeaOj)  

Alumina  (AlaO3) 

Oxide  of  nickel  (NiO) 

Lime  (CaO)  .'. 

35-5 
13.0 

32.7 
11.4 

Magnesia  (MgO)     . 

Potash  (K?O) 

Chlorine(Cl)  

65.4 
3-1 
44  o 

39-9 
4.8 
43.0 
18.0 

39-9 
5-o 
29.8 
24.3 
Trace. 

10.7 
22.3 

20.8 

19.4 

Trace. 

6.4 
16.9 
19.7 
28.2 

1.2 

8.2 

ii.  6 
25-9 
37-4 
Trace. 

5.6 
14-7 
21.3 

23-3 
1.6 

10.4 
3-3 
38.7 
18.1 

3-7 

10.4 
33 
38.7 
18.3 
Trace. 

Nitric  acid  (NjO»)     . 

Carbonic  acid  (combined)  (CO*).  ... 

P                        »    0 

WATER   PURIFICATION  AT  LOUISVILLE. 


BIOLOGICAL  CHARACTER  OF  THE  OHIO 
RIVER  WATER. 

Determinations  of  the  number  of  bacteria 
in  the  river  water,  and  a  study  of  their  relation 
to  disease,  occupied  the  gerater  part  of  the  at 
tention  with  regard  to  this  portion  of  the  work. 
Microscopical  examinations  of  the  water, 
however,  were  made  from  time  to  time  to 
learn  the  numbers  and  kinds  of  the  larger 
micro-organisms  which  were  present. 

Microscopical  Examinations  of  the  River  Water. 

In  the  next  table  (see  p.  37)  there  are  pre 
sented  the  results  of  the  microscopical  exam 
ination  of  the  river  water  for  the  presence  of 
algae,  diatoms,  etc.  As  already  stated,  these 
micro-organisms  are  much  larger  than  the 
bacteria,  and  may  be  classified  by  the  aid  of 
low  powers  of  the  microscope. 

It  will  be  noted  that  the  algae  (cyanophyeae 
and  chlorophyceae)  and  diatoms,  which  are 
visually  abundant  in  surface  water  during  hot 
weather,  were  present  in  only  very  limited 
numbers  after  the  last  of  May,  1896.  The 
reason  of  this  was,  undoubtedly,  that  the  large 
amount  of  suspended  matter  in  the  water 
prevented  the  sunlight,  which  is  necessary  for 
their  development,  from  reaching  them. 

In  1897  no  microscopical  examinations  of 
the  river  water  were  made  during  its  muddy 
condition.  The  single  analysis  on  June  n, 
however,  when  the  water  was  very  clear,  com 
paratively  speaking,  shows  the  range  in  num 
bers  and  kinds  of  organisms  which  may  be 
expected  under  such  conditions. 

Identification  of  Species  of  Bacteria  in  the  River 

Water,  -with  special  reference  to  their 

Causation  of  Disease. 

With  regard  to  this  portion  of  the  biologi 
cal  analyses  attention  was  especially  directed 
to  the  detection  of  bacteria  which  are  dan 
gerous  or  suspicious  from  a  hygienic  point  of 
view.  It  is  to  be  stated  that  during  the  low 
water  in  the  river  in  November,  1895,  and 
again  during  the  last  part  of  April  and  early 
part  of  May,  1896,  when  there  had  been  a 
drought  for  a  month  or  more,  there  was  found 
in  the  river  water  B.  coli  communis.  This 


germ  is  the  most  prominent  one  in  sewage, 
and  it  is  also  the  most  abundant  species  in  the 
fecal  discharges  of  man  and  certain  domestic 
animals.  On  May  i,  five  days  after  the  be 
ginning  of  the  period  when  this  germ  was  re 
peatedly  found  in  the  river  water,  an  exam 
ination  of  the  tap  water  in  the  city  also 
showed  its  presence  there. 

At  high  stages  of  the  river  and  when  the 
water  was  very  muddy  the  results  of  numer 
ous  examinations  for  sewage  bacteria  were 
negative  in  a  great  majority  of  cases. 
Nevertheless,  B.  coli  communis  was  found  in 
the  river  water  on  June  30,  1896,  and  closely 
allied  kinds  of  bacteria  were  noted  from  time 
to  time  during  the  investigations.  The  evi 
dence  indicates  that  with  muddy  water  and 
high  stages  of  the  river  there  are  conditions 
which  aid  in  causing  the  disappearance  to  a 
marked  degree  of  those  germs  which  appear 
to  come  from  the  entrance  of  sewage  into  the 
river  above  the  pumping  station. 

The  results  of  tests  for  the  presence  of  the 
germs  of  typhoid  fever  and  other  diseases 
were  negative  in  all  cases.  It  is  not  to  be 
understood,  however,  that  these  negative  re 
sults  are  adequate  proof  that  disease  germs 
were  entirely  absent  from  the  river  water. 

The  reason  of  this  lies  in  the  natural  limita 
tion  of  the  most  approved  laboratory  methods, 
which  at  best  allow  an  examination  of  only 
a  very  small  portion  of  the  quantity  of  water 
flowing  in  the  stream.  These  comments  are 
especially  true  in  view  of  the  fact,  as  stated 
above,  that  at  times  of  low  water  there  were 
present  intestinal  bacteria. 

In  1897  twelve  tests  for  B.  coli  communis 
were  made  between  January  2 1  and  February 
4,  with  negative  results  in  each  case.  From 
April  i  to  9,  nine  more  tests  were  made  in 
which  this  germ  was  found  in  three  instances. 

The  question  of  the  classification  of  the  nu 
merous  but  harmless  species  of  bacteria  in  the 
writer  received  as  much  attention  as  time  al 
lowed.  Owing  to  the  fact  that  there  were 
several  other  lines  of  work  which  yielded  re 
sults  of  greater  importance  from  a  practical 
standpoint,  this  question  was  not  made  one  of 
constant  study.  Nevertheless,  the  investiga 
tions  on  the  detection  of  dangerous  or  suspi 
cious  species,  and  on  the  comparison  of  the 
species  of  bacteria  in  the  water  before  and 


COMPOSITION  OF  OHIO  RIVER    WATER. 


RESULTS   OF    MICROSCOPICAL   ANALYSES   OF   THE   OHIO    RIVER   WATER. 
(Number  of  organisms  per  cubic  centimeter.) 


Date  of  Collection. 

1 

1896. 
February. 

1896. 

March. 

•896. 
April. 

1896. 
May. 

1846. 

June. 

1896. 
July. 

8 

1897. 
lunc. 

•jj    ,6 

4 

,, 

19 

Number  of  Sample. 

277 

2801 

304    329 

354 

382 

404 

459 

471 

516    544 

564     585     629 

651    684 

711  jooi 

D' 

340 

ft 

60 

18 

38 

112    44 

6 

24           2           2 

659 
"5 
69 

165 
37 

16 

96 

60, 

8 

8 

9 

16 

5 

40 

40 

8 

M 

16      8 

6 

16 

2 

2 

Tabellaria  

So 
I 
173 

I 

8 

3 

g 

Cyclotella     

20 

20 

8 

2 

g 

-.2        8 

g 

g 

ft 

I 
I 
17 
8 
8 
289 

2O 

o 

8 

2 

I 

8 

o 

o 

2 

8 

26 

352     20 

4 

16        2 

O 

g 

22 

88 

8 

g 

26 

20 
M3 
2 
'3 
0 

19 
I 
2 
13 

g 

O 

60 
60 

20 

8 
8 
at 

2 
2 
2 

2 
2 
3 

12 
12 
6 

10 
IO 
0 

8 
8 
16 

2 
2 
O 

0          2 

0        0 

O 

0          0 

2 
2 
2 

o 

6    |      2 

8     20 

'4 

24           2 

4 
IO 

8 
8 

2 

2 

8 

8    16 

Cilliata  

g 

2 

8 

3 

o 

o 

0 

4 

2 

O 

o 

0 

2 

0 

o 

o      8 

o 

16 
g 

O 

O 

I 

13 
I 

i 
3 
2 
I 

Rotifera    

g 

40 

0 

8 

2 

2 

3 

o 

0 

12         4 

24      8 
16  .  .  .  . 

6 
6 

O          0 

0 

Ova  

8 

2 

8      4 

IO 

44 
7 

2 
72 
IO 

400 

6 
Ver 

200 

5 
y  abi 

168 
8 
nda 

28 
10 
nt  in 

II 

all  c 

70 
'3 
ases. 

21 

5 

168 

8 

66 

IO 

496    96 
8      9 

3° 

5 

80 

9 

6 
3 

6 
3 

993 
26 

Amorphous  matter  

after  purification,  necessarily  involved  a  con 
siderable  effort  in  this  direction.  Comparison 
of  the  results  of  diagnostic  tests  used  for  the 
identification  of  species  of  bacteria  with  the 
available  published  descriptions  of  bacteria 
indicated,  so  far  as  the  similarity  of  labo 
ratory  methods  would  allow,  the  presence 
of  several  new  species  as  well  as  a  consider 
able  number  which  have  been  found  else 
where. 

The  following  list  of  bacteria  and  yeasts, 
together  with  the  results  of  the  microscopical 
examinations  already  presented  in  this  chap 


ter,  indicate  the  nature  of  the  microscopic 
llora  of  the  Ohio  River  water: 

Bacillus  arborescens  (Frankland). 
aurantiacus  (Frankland). 
coli  communis  (Kscherich). 
flavescens  (Pohl). 
fluorescens  liquefaciens  (Fliigge). 
fluorescens    non-liquefaciens    (Ei- 

senberg). 

fulvus  (Zimmerman). 
"        janthinus  (Zopf). 

lactis  serogenes  (Escherich). 
"        mesentericus  ruber  (Globig). 


WATER  PURIFICATION  AT  LOUISVILLE. 


Bacillus  nebulosus  (Wright). 

prodigiosus  (Ehrenberg). 

proteus  vulgaris  (Hauser). 
"       radiatus  aquatilis  (Zimmerman). 
"       ramosus  (Frankland). 
"       rubidus  (Eisenberg). 
"       subtilis  (Ehrenbcrg). 
"       venenosus  (Vaughan). 
"       violaceus  (Frankland). 


Cladothrix  castrana  (Cohn). 

dichotoma  (Cohn). 
Micrococcus  aquatilis  (Bolton). 

cremoides  (Zimmerman). 
Proteus  fluorescens  (Jager). 
Sarcina  lutea  (Schroeter). 
Saccharomyces  cerevisoa  (Mayen). 
Rosa  Hefe. 


COMPOSITION  OF  OHIO  RIVER    WATER. 


39 


Quantitative   Bacterial   Analyses    of  the    River    Water. 

The  average   results   for  each   day  of   the   determination  of    the  numbers  of  bacteria  in  the 
river  water  are  recorded  in  the  following  table: 

AVERAGE    RESULTS   OF    DAILY    DETERMINATIONS    OF    THE    NUMBER   OF    BACTERIA    PER 
CUBIC   CENTIMETER    IN    THE   OHIO    RIVER    WATER. 


Date. 

October. 

November. 

December. 

January. 

February. 

March. 

April. 

May. 

Jun. 

1  8  800 

6  800 

8  600 

126 

6 

228 

8 

l87 

637 

6600 

888 

3  600 

800 

1  80 

16 

I  6  600 

18 

1  66 

184 

4  Soo 

d8 

D 

58 

8  ooo 

18 

8  i(x> 

28 

^8 

06 

12  (XX) 

81 

*  ' 

^uo 

_ 

Date. 

July. 

August. 

December. 

February. 

March. 

April. 

May. 

jun. 

July. 

-4 

5 

g 

' 

8  700 

" 

8  300 

16 

t  Soo 

6fio 

18 

1  1  800 

46    8OO 

6  loo 

26 

28 

8  600 

4° 


WATER   PURIFICATION  AT  LOUISVILLE.. 


CHAPTER   II. 

DESCRIPTION     OF     THE     APPLICATION     OF  CHEMICALS    TO     THE 
WATER  BY  THE  SEVERAL  SYSTEMS  OF  PURIFICATION. 


OHIO     RIVER 


WITH  the  systems  of  purification  examined 
during  the  first  portion  of  these  tests,  the  ap 
plication  of  chemicals  is  a  matter  of  funda 
mental  importance  for  two  reasons: 

1.  Chemicals  are  absolutely  necessary  un 
der  normal  conditions  for  successful  filtration 
of  water  through  sand  at  the  rapid  rate  em 
ployed  in  American  filters. 

2.  The  application  of  chemicals  to  facilitate 
the  subsidence  of  suspended  matters,  in  such 
muddy  water  as  that  of  the  Ohio  River,  and 
to  insure  efficient  filtration,  makes  their  use 
the  principal  item  in  the  cost  of  purification 
of  this  water  by  these  systems. 

The  topics  which  are  considered  in  this 
chapter  are  as  follows: 

Kinds  of  chemicals  used. 

Composition  of  chemicals. 

Effect  of  the  application  of  alum,  or  sul 
phate    of   alumina,    to    the    Ohio    River  j 
water. 

Devices  used  by  the  respective  systems  for 
the  application  of  chemicals  to  the  Ohio 
River  water. 

Uniformity  in  the  rate  of  application  of 
chemicals  by  the  respective  devices. 

Strength  of  solutions  of  chemicals  applied 
to  the  river  water  by  the  respective  sys 
tems. 

Average  daily  amounts,  in  grains  per  gal 
lon,  of  sulphate  of  alumina  applied  to  the 
river  water  by  the  respective  systems. 

This  chapter  deals  with  the  problem  as  it 
stood  on  Aug.  i,  1896. 

KINDS  OF  CHEMICALS  USED. 

During  these  tests  (1895-96)  three  kinds  of 
chemicals  were  used: 

i.  Sulphate  of  alumina  (trade  name,  "  basic 
sulphate  of  alumina  "). 


2.  Potash  alum. 

3.  Lime. 

Electrolytically  formed  chlorine  and  scrap- 
iron  were  also  used  in  an  experimental  way 
with  the  Jewell  System  for  a  few  hours  on 
each  of  several  days. 

Sulphate  of  alumina,  of  different  lots  and 
brands,  was  used  regularly  in  the  Warren  and 
Jewell  systems,  except  for  a  few  hours  on 
Feb.  TO  in  the  case  of  the  Warren  System, 
when  potash  alum  was  employed.  During 
the  time  when  the  Western  Company  made 
use  of  their  first  device  for  the  application  of 
chemicals,  potash  alum  was  used  instead  of 
sulphate  of  alumina,  because  the  former  was 
less  soluble  in  water,  and  therefore  more 
adaptable  under  the  circumstances,  as  will  be 
shown  beyond. 

Potash  alum  was  used  by  the  Western  Sys 
tem  up  to  May  20,  and  from  June  4  to  6, 
inclusive.  Sulphate  of  alumina  was  used  dur 
ing  the  remainder  of  the  test. 

During  a  greater  part  of  the  time  from 
Feb.  8  to  April  i ,  inclusive,  lime  was  added 
to  the  river  water  with  the  sulphate  of  alu 
mina  in  the  case  of  the  Jewell  System.  The 
object  of  this,  apparently,  was  to  improve  the 
effect  of  the  application  of  the  sulphate  of 
alumina,  and  to  guard  against  the  passage  of 
the  latter  through  the  system  into  the  filtered 
water. 

Sulphate  of  alumina,  known  commercially 
as  basic  sulphate  of  alumina,  and  potash  alum 
are  approximately  of  equal  cost.  The  former 
contains  no  potash,  less  sulphuric  acid  and 
water  of  crystallization,  but  more  alumina,  as 
is  shown  in  the  table  of  analyses  in  the  next 
section.  It  is  the  available  (soluble  in  water) 
alumina  in  these  two  chemicals  which  give  to 
them  their  efficiency  in  connection  with  the 
purification  of  such  water  as  that  of  the  Ohio 


APPLICATION  OF   CHEMICALS    TO    THE   OHIO   RIVER    WATER. 


River.  For  this  reason  sulphate  of  alumina 
is  better  and  more  economical  to  employ  for 
this  purpose. 

COMPOSITION  OF  CHEMICALS. 

The  average  results  of  duplicate  analyses 
of  potash  alum  crystals  used  in  the  Western 
System,  as  stated  above,  are  presented  in  the 
following  table.  For  the  purpose  of  com 
parison  the  theoretical  percentage  composi 
tion  of  pure  potash  alum  is  also  given. 

PERCENTAGE     COMPOSITION     OF     POTASH  . 
ALUM   USED   IN   THE  WESTERN  SYSTEM. 


Source  of  Sample. 

Alum  Used  in 
Western 
System. 

Pure  Alum 
(theoretical). 

Matter  insoluble  in  water  
Available  alumina  (AljOj).  .  .  . 
Sulphuric  acid  (SO3)   

O.O2 
10.72 
34.06 
45.69 
IO.OO 

o 

o.oo 

10.77 

33-76 

45-54 
9-93 

0 

o 

Water(HjO)         

Potash  (KjO)   

Lime  (CaO)  

Oxide  of  iron  (FeiOj)   

These  results  show  that  the  potash  alum 
used  in  the  Western  System  was  absolutely 
pure,  practically  speaking. 

In  the  next  table  are  presented  results  of 
analyses  of  the  sulphate  of  alumina  used  in 
the  several  systems.  In  the  Warren  System 
use  was  made  of  one  brand  obtained  in  three 
principal  lots.  For  the  most  part  in  the  Jewell 
System  use  was  made  of  one  brand,  but  a 
different  one  from  that  of  the  Warren  Sys 
tem,  and  also  obtained  in  three  principal  lots. 
The  second  brand  (lot  No.  4)  was  used  in  the 
Jewell  System  alternately  with  the  regular 
brand  from  June  20  to  30,  inclusive,  and  from 
July  6  to  ii,  inclusive.  With  the  Western 
System  use  was  made  of  several  lots,  for  the 
most  part  of  the  same  brand  as  that  employed 
in  the  Warren  System. 

In  order  to  compare  the  composition  of 
these  commercial  products  with  that  of  the 
theoretical  sulphate  of  alumina,  the  percent 
age  composition  of  the  latter  is  given  in  the 
following  table: 


PERCENTAGE   COMPOSITION   OF   THE   SEVERAL   LOTS   OF   SULPHATE.   OF   ALUMINA. 


System. 

Number 
of 
Lot. 

Matter 
Insoluble  in 
Water. 

Available 
Alumina 
(Al,0,). 

Sulphuric 
Acid  (SO3). 

Water 

(Ha(J). 

Timrirnm     Oxide  of  Iron 
(KejO,). 

I 
2 
3 

1 

2 

3 
4 

2 

o.oO 
0.  IO 
O.O2 
1.9S 
0.63 

0.4" 

2.  17 
0.30 
0.00 

17.88 
17.90 
17.86, 

16.39 

16.19 

if).  12- 
lS.62 
17.20 

"5-32 

39-87 
38.61 
37-72 
37-  96 
37-87 
37--4S 
42.20 
37-64 
36.04 

41  .22 
42-75 
44.62 
43.46 
45-28 
46.08 
36  .  90 
44-92 
48.64 

o.oo 
Trace 
0.08 

Trace 
Trace 
Trace 

0.02 
O.OO 

0.43 
0.32 
o.oo 
0.20 
0.1X3 
O.OO 

"•34 

0.24 

o.oo 

,. 

lewell 

,. 

Western                                      

Sulphate  of  alumina  (theoretical).. 

In  connection  with  the  above  tables  it  is 
to  be  noted  that  each  lot  of  commercial 
sulphate  of  alumina  contained  considerably 
more  available  alumina  than  the  theoretical 
sulphate  of  alumina.  It  is  this  portion  (avail 
able  alumina)  of  these  compounds  that  gives 
to  them  their  efficiency  for  this  particular  pur 
pose;'  and,  on  an  average,  these  commercial 
products  contained  about  60  per  cent,  more 
available  alumina  than  the  pure  potash-alum 
crystals,  analyses  of  which  are  presented  in  a 
foregoing  table.  Some  of  the  sulphate  of 
alumina  used  in  the  Jewell  System  contained 
more  alumina  than  is  indicated  by  the  above 
results.  But  as  it  was  insoluble  in  water  it 
was  of  no  value,  and  is  recorded  with  other 
matters  as  "  matter  insoluble  in  water." 


These  lots  of  sulphate  of  alumina  differed  in 
part  from  the  theoretical  sulphate  of  alumina, 
in  that  they  contained  less  water  of  crystalliza 
tion  owing  to  the  process  of  their  prepara 
tion.  This  fact  alone  caused  the  former  to 
be  richer  in  available  alumina  than  the  latter. 
The  increase  in  the  available  alumina  in  the 
commercial  products  above  that  in  the  theo 
retical  sulphate  of  alumina  was  also  greater 
than  the  corresponding  increase  in  sulphuric 
acid.  This  point  doubtless  explains  the 
origin  of  the  trade  name,  basic  s.ulphate  of 
alumina.  The  ratio  of  the  alumina  (A12O3) 
to  the  acid  (SO3)  in  each  lot  is  shown  in  the 
following  table,  with  the  corresponding  ratio 
in  the  theoretical  sulphate  of  alumina  taken 
as  one: 


4-' 


WATER  PURIFICATION  AT  LOUISVILLE. 


System.        Lot. 

Warren  .  .    i 
.  .   2 


Ratio. 

1.05 
1.09 


Western  .   2       1.07 


System.         Lot.  Ratio. 

Jewell.  .  .    i        i. 02 

"         ...     2          I.OI 

...   3       i.oi 

"       ...   4       1.04 


In  all  comparisons  and  tabulations 
throughout  this  report  the  chemicals  applied 
to  the  river  water  for  the  purpose  of  coagula 
tion  and  sedimentation  are  expressed  in  terms 
of  sulphate  of  alumina.  Wherever  potash 
alum  was  used  the  results  are  converted  into 
their  respective  equivalents  of  sulphate  of 
alumina,  on  the  basis  that  10  parts  of  the  lat 
ter  are  equal,  from  a  practical  point  of  view, 
to  1 6  parts  of  potash  alum. 

EFFECT  OF  THE  APPLICATION  OF  ALUM  OR 

SULPHATE  OF  ALUMINA  TO  THE  OHIO 

RIVER  WATER. 

When  alum  or  sulphate  of  alumina  is  ap 
plied  to  the  Ohio  River  water,  it  is  decom 
posed  for  the  most  part  by  the  lime  (calcium 
carbonate  and  bicarbonate)  dissolved  in  the 
water,  and  there  is  formed  a  white,  gelatinous 
precipitate  of  aluminum  hydrate.  The  mag 
nesium  carbonate  and  bicarbonate  in  the 
water  also  decompose  the  alum  in  the  same 
manner  as  does  the  lime.  Carbonic  acid  gas 
is  liberated  by  the  decomposition  of  the  alum, 
but  remains  dissolved  in  the  water  as-  free 
acid.  The  lime  and  magnesia  which  combine 
with  and  decompose  the  alum  pass  into  the 
form  of  soluble  neutral  sulphates.  The  tiny, 
sticky  particles  of  aluminum  hydrate  group 
themselves  together;  and  around  the  infinite 
number  of  centers  of  coagulation  are  gathered 
together  more  or  less  completely  the  matters 
suspended  in  the  water,  including  the  bac 
teria,  thereby  forming  flakes  of  greater  or  less 
size  and  weight.  Neither  before  or  after  its 
decomposition  has  the  alum  or  sulphate  of 
alumina,  in  amounts  which  would  be  permis 
sible  in  the  purification  of  municipal  water 
supplies,  a  germicidal  effect  on  the  bacteria, 
but  simply  aids  in  their  removal,  through  sub 
sidence  and  filtration,  by  their  envelopment 
in  the  gelatinous  flakes.  Several  factors  ex 
erted  a  marked  influence  upon  the  coagula 
tion,  upon  the  subsequent  sedimentation,  and 
finally  upon  the  effect  of  the  remaining  co- 


agula  in  the  water  as  it  was  filtered  at  a  rapid 
rate  through  the  sand. 

The  application  of  chemicals  to  the  Ohio 
River  water  where  this  system  of  purification 
is  employed  is  of  fundamental  importance,  in 
fluencing  both  the  efficiency  and  cost  of  the 
system,  and  the  whole  subject  in  its  different 
phases  will  be  discussed  in  detail  beyond.  At 
this  time  it  is  the  purpose  simply  to  point  to 
the  matter  in  a  very  general  way,  in  order  to 
make  plainer  and  to  bring  out  the  signifi 
cance  of  the  following  account  of  the  devices 
used  in  the  initial  step  in  the  process  of  puri 
fication. 

DEVICES  USED  IN  THE  RESPECTIVE  SYSTEMS 

FOR  THE  APPLICATION  OF  CHEMICALS 

TO  THE  OHIO  RIVER  WATER. 

In  this  section  is  given  a  brief  description 
of  the  principal  features  of  the  several  devices 
for  the  application  of  solutions  of  alum  and 
other  chemicals.  An  account  of  the  effi 
ciency  with  which  this  was  accomplished  will 
be  found  in  subsequent  sections  of  this  chap 
ter.  In  the  following  chapters  are  described 
the  decomposition  and  subsequent  disposi 
tion  of  the  applied  alum  or  sulphate  of  alu 
mina,  and  also  the  effect  which  this 
application  produced  in  connection  with  the 
purification  of  water. 

Warren  Device. 

Sulphate  of  alumina  was  applied  to  the 
water  in  the  Warren  System  just  after 
the  river  water  entered  the  settling  basin. 
The  current  of  water  in  the  inlet  water- 
pipe  revolved  a  small  propeller  wheel  lo 
cated  in  the  mouth  of  the  pipe.  This  wheel 
turned,  by  means  of  two  sets  of  beveled  gears, 
a  specially  designed  pump,  working  in  a 
pump  box  on  the  floor  above.  This  pump 
box  received  the  sulphate  of  alumina  solution 
from  the  mixing  tanks,  the  flow  from  which 
was  regulated  by  a  float  valve.  From  the 
pump  the  solution  of  sulphate  of  alumina 
passed  through  a  lead  pipe  discharging  by 
gravity  into  the  water  in  the  settling  basin, 
opposite  the  center  and  approximately  5 
inches  from  the  end  of  the  inlet  water-pipe. 

Two  white-pine  mixing  tanks  were  located 
on  the  floor  over  the  settling  basin  and  ad- 


APPLICATION   OF  CHEMICALS    TO    THE   OHIO   RIVER    WATER. 


43 


jacent  to  the  pump  box.  These  tanks  were 
used  alternately,  solutions  being  made  up  in 
one  tank  while  the  other  was  in  service.  Fil 
tered  water  pumped  from  the  filtered-water 
reservoir  was  used  for  dissolving  the  sulphate 
of  alumina;  and  stirring  was  done  in  all  cases 
by  hand.  The  depth  of  the  tanks  was  4.5 
feet  and  the  diameter  about  4  feet.  Owing 
to  unsatisfactory  working  of  the  meter  on  the 
pipe  through  which  the  chemicals  entered  the 
water,  and  its  final  abandonment,  glass 
gauges  were  employed  for  measuring  the 
quantity  of  solution  used.  Calibrations  of  the 
tanks  showed  an  average  capacity  for  each 
o.i  foot  in  depth  of  1.24  and  1.18  cubic  feet 
in  tanks  A  and  B,  respectively.  Owing  to  the 
distance  which  the  outlet  pipe  was  above  the 
floor  of  the  tanks,  the  lower  portion  of  the  so 
lution  in  the  tanks  could  not  be  used.  The 
quantity  of  solution  left  in  the  tanks  each 
time  a  new  solution  was  prepared  varied  con 
siderably,  but  generally  amounted  to  some 
thing  less  than  3  cubic  feet. 

Pump  Box. — The  solution  of  sulphate  of 
alumina  flowed  into  the  pump  box  from  the 
mixing  tanks,  the  flow  being  regulated  by  a 
2-inch  float  valve  of  vulcanized  rubber.  The 
pump  box  was  about  2.9  feet  long  by  1.2  feet 
wide.  The  depth  of  solution  in  the  pump 
box  was  capable  of  regulation  by  varying  the 
distance  of  the  float  from  the  center  of  the 
valve,  the  float  arm  being  adjustable  in 
length.  This  was  intended  as  a  means  of 
varying  the  rate  of  application  of  solution  by 
increasing  or  decreasing  the  depth  of  immer 
sion  of  the  pump  arms.  In  practice  it  was 
not  found  successful,  as  the  float  valve  was 
too  irregular  to  make  such  an  adjustment 
feasible.  The  maximum  and  minimum  depths 
of  solution,  at  the  overflow  of  the  pump  box 
and  the  lowest  level  at  which  the  device  op 
erated,  were  1 1  and  5  inches,  respectively. 

Propeller. — The  propeller  wheel  was  a 
small  screw  wheel  of  about  0.5  foot  outside 
diameter,  set  on  a  horizontal  shaft  directly 
in  the  mouth  of  the  inlet  water-pipe.  When 
the  Warren  System  was  first  installed  a 
5-blade  wheel  was  tried,  but  this  was  taken 
out  and  a  7-blade  wheel  substituted  Nov.  25, 
1895.  This  wheel  was  made  of  cast  brass. 
0.5  foot  in  diameter  by  0.2  foot  deep.  There 
were  seven  blades,  each  pitched  so  that  the 


circumferential  distance  between  their  edges 
was  2  inches.  Connections  from  this  pro 
peller  wheel  to  the  shaft  of  the  chemical  pump 
above  were  made  by  two  sets  of  small  beveled 
gears  and  a  vertical  shaft. 

Pump. — The  pump  was  a  patented  device 
constructed  of  vulcanized  rubber.  It  was 
made  up  of  six  hollow  curved  arms,  each  of 
which  lay  in  a  plane  perpendicular  to  the 
horizontal  shaft  on  which  the  pump  revolved, 
and  which  were  connected  respectively  to  six 
tubes  placed  parallel  to  the  same  shaft.  The 
shape  of  the  curved  arms  was  approximately 
that  of  two  straight  pipes  5  and  3  inches  long, 
respectively,  making  an  angle  of  45°  and  con 
nected  by  a  circular  curve  of  3  inches  radius. 
The  inside  diameter  of  these  arms  and  of  the 
horizontal  tubes  was  0.5  inch.  In  operation 
the  pump  was  revolved  by  the  propeller 
wheel  just  described.  The  shaft  of  the  pump 
was  located  upon  the  top  of  the  pump  box, 
the  solution  filling  the  pump  box  ordinarily 
to  from  I  to  3  inches  below  the  pump  shaft. 
As  the  pump  revolved,  each  arm  was  filled 
as  it  entered  the  solution,  and  as  the  end  was 
the  first  part  to  leave  the  solution  it  trapped 
some  of  it,  the  amount  varying  with  the 
height  of  the  solution  in  the  box.  As  the 
pump  turned  the  liquid  was  dropped  back  into 
the  arm  and  emptied  out  of  the  horizontal 
tube  into  a  funnel  at  the  side  of  the  box.  To 
this  funnel  was  connected  a  lead  pipe  through 
which  the  solution  flowed  into  the  settling 
basin,  discharging  opposite  the  mouth  of  the 
inlet  water-pipe. 

Manner  of  Control  of  the  Application  of 
Chemicals. — When  the  flow  of  river  water. 
into  the  settling  chamber  was  not  too  low 
(above  18  cubic  feet  per  minute)  the  discharge 
of  the  solution  from  the  pump  was  supposed 
to  be  proportional  to  the  admission  of  river 
water.  The  amount  of  solution  pumped  was 
changed  by  the  removal  or  insertion  of  rub 
ber  stoppers  into  the  ends  of  the  hollow  arms 
of  the  pump.  In  some  instances  half-stop 
pers  (halved  lengthwise)  were  inserted. 
Marked  changes  in  the  application  of  alum 
called  for  new  solutions  of  different  strength. 

Elevations. — The  relative  elevations  in  feet 
of  the  more  important  points,  referred  to  the 
bottom  of  the  sand  layer  of  the  filter  as  the 
datum  plane,  were  as  follows: 


44 


IVATER   PURIFICATION   AT  LOUISVILLE. 


Maximum  flow  line  in  mixing  tanks..  14.80 
Minimum  flow  line  in  mixing  tanks.  .  .  .  10.66 

Center  of  chemical  pump 10.60 

Maximum  flow  line  in  pump  box 10.58 

Center  of  discharge  in  the  settling  basin .    1.03 

Jeivell  Device. 

The  solution  of  sulphate  of  alumina  was 
pumped  into  the  inlet  water-pipe  against  a 
pressure  of  about  60  pounds  at  a  point  about 
lofeet  inside  the  settling  chamber.  Before  the 
entrance  to  the  settling  chamber  of  the  river 
water  containing  the  solution  it  passed  through 
a  meter  and  two  valves  on  the  main  inlet  pipe. 
Mixing  Tanks. — Sulphate  of  alumina  solu 
tions  were  prepared  alternately  in  two  cypress 
tanks  5.5  feet  deep  and  3.5  feet  in  average 
diameter.  Filtered  water,  taken  from  the 
outlet  pipe  just  as  it  left  the  filter,  was  used 
for  dissolving  the  commercial  product  after 
it  had  been  broken  into  small  pieces.  This 
was  facilitated  at  times  by  heating  the  water 
with  steam  which  was  allowed  to  enter  the 
water-pipe  just  before  it  reached  the  tanks. 
Pump. — From  *he  tanks  the  solution  was 
pumped  into  the  inlet  pipe  by  a  3.5  by  4.5  by 
6-inch  single  pump,  the  suction  pipes  of  which 
reached  to  within  about  i  inch  of  the  bottom 
of  the  tanks.  The  ends  of  the  suction  pipes 
were  capped  with  screens.  The  steam  supplied 
to  the  pump  was  kept  at  practically  a  constan'. 
pressure  by  means  of  a  regulating  valve. 

Feed  Pipe. — The  feed  pipe  from  the  pump 
to  the  inlet  pipe  was  a  heavy  lead  pipe  0.75 
inch  in  diameter.  At  first  all  fittings  were  of 
wrought  iron,  but  owing  to  corrosion  by  the 
sulphate  of  alumina  they  repeatedly  broke, 
and  at  the  close  of  the  test  practically  all  fit 
tings  were  of  brass. 

Manner  of  Control. — At  the  outset  it  was 
the  custom  to  start  the  pump  at  a  speed  to 
deliver  the  desired  quantity  of  solution  and 
keep  it  under  general  control  by  means  of  a 
float  on  the  water  above  the  sand  layer.  This 
float  was  connected  by  a  chain  and  pulley 
with  a  valve  regulating  the  flow  of  steam  to 
the  pump.  This  was  not  a  success,  and  the 
float  was  abandoned  during  the  latter  part  of 
March,  and  the  application  controlled  by  fre 
quent  regulations  of  the  steam-valve,  inspec 
tions  of  quantities  from  the  meters  and  of  the 
speed  of  the  pump  being  used  as  guides. 


Ordinarily,  changes  in  the  speed  of  the  pump 
would  allow  the  desired  arrangement  in  the 
application  of  sulphate  of  alumina,  but  in  ex 
treme  cases  the  strength  of  the  solution  was 
altered. 

Elevations. — The  relative  elevations  in  feet 
of  the  more  important  points,  with  the  bot 
tom  of  the  sand  layer  of  the  filter  as  the  datum 
plane,  were  as  follows: 

Maximum  flow  line  in  mixing  tanks.  -  6.90 
Minimum  flow  line  in  mixing  tanks.  -  12.06 
Center  of  discharge  into  inlet  pipe.  .  -  11.13 

Western  Systems. 

As  only  one  settling  chamber  was  used  for 
both  the  Western  Pressure  and  Western 
Gravity  systems  a  single  device  for  the  appli 
cation  of  alum  was  sufficient.  Two  separate 
and  distinct  devices,  however,  were  used. 
The  first  was  used  from  the  beginning  of  the 
operation  of  these  systems  up  to  April  7,  and 
the  second,  following  an  extended  period  of 
modifications  and  repairs,  was  in  service  from 
May  7  till  the  close  of  the  tests. 

First  Western  Device. 

On  the  main  inlet  water-pipe  to  the  set 
tling  chamber  there  was  a  6-inch  gate 
valve  which  caused  a  difference  in  pres 
sure  above  and  below  it.  From  above  this 
valve  a  o.5-inch  brass  pipe  led  to  the  alum 
tank,  which  was  a  cast-iron  vertical  cylinder 

1  foot  in  inside  diameter  and  approximately 

2  feet  deep.     The  alum  tank  had  a  top  open 
ing  with  a  cover  constructed  like  a  hand-hole 
fitting.      The  diameter  of  the  opening  was 
4.5  inches.     The  brass  pipe  above  mentioned 
connected  with  the  alum  tank  at  the  top  and 
extended  into  it  about  I  foot.  From  the  top  of 
the  alum  tank  a  second  o. 5-inch  brass  pipe  led 
to  the  inlet  pipe  below  the  valve  above  men 
tioned.      Suitable  valves  cut  off  the  flow  in 
both  brass  pipes;   allowed  access  to  the  alum 
tank;  and  aided  in  controlling  the  flow  of  alum 
solution.     A  mercury  column  in  a  celluloid 
tube  was  used  to  indicate  the  difference  in 
pressure  in  the  two  brass  pipes.      By  this  ar 
rangement  the  alum  solution  was  applied  to 
the  river  water  in  the  inlet  pipe  about  10  feet 
from  the  settling  chamber. 

Operation. — In  use  the  alum  tank  was  kept 
filled  to  a  greater  or  less  depth  with  crystals 


APPLICATION  OF  CHEMICALS    TO    THE   OHIO   RIVER    WATER. 


45 


of  potash  alum  put  in  through  the  hand-hole 
at  the  top.  Differences  in  pressure  in  the 
inlet  water-pipe  before  and  after  this  by-pass 
caused  the  flow  of  a  small  quantity  of  water 
through  the  tank  whereby'  the  alum  was  dis 
solved  and  carried  over  into  the  inlet  water- 
pipe.  The  only  means  of  regulating  the 
quantity  of  alum  solution  applied  was  by  dif 
ferences  in  the  pressure  of  the  water  flowing 
through  this  by-pass. 

Second  Western  Dei-ice. 

The  entire  device  for  the  application  of 
chemicals  was  changed  during  April,  the  final 
arrangement  being  as  follows: 

The  separate  pipe  for  the  admission  of  river 
water  to  the  system,  which  was  introduced 
Feb.  29,  was  broken  and  a  duplex  pumping 
engine  inserted  on  the  pipe  line.  To  this  du 
plex  pump  were  attached  auxiliary  pumps  by 
which  the  solution  of  chemicals  was  forced 
into  the  main  inlet  water-pipe  beyond  the 
pumps  and  about  30  feet  from  the  settling 
chamber.  The  duplex  water  pump  forced 
the  river  water,  containing  the  alum  or  sul 
phate  of  alumina  solution,  through  the  set 
tling  chamber,  and  also  through  the  pressure 
filter,  or  into  the  top  of  the  gravity  filter. 

Mixing  Tanks.— Two  pine  tanks  each  4  feet 
deep  by  3  feet  in  diameter  were  used  alter 
nately  for  the  purpose  of  preparing1  the  solu 
tions.  The  solutions  were  made  with  filtered 
water  taken  from  the  outlet  pipe  near  its  exit 
from  the  pressure  filter,  or  with  river  water 
when  the  pressure  filter  was  not  in  operation. 

Afain  Water  Pumps. — The  main  pumping 
engine  was  a  Worthington  single-expansion 
duplex  engine.  The  principal  dimensions 
were  as  follows: 

Diameter  of  steam  cylinder 9  inches 

Diameter  of  water  cylinder 8.5 

Length  of  stroke 10 

Steam  was  supplied  by  a  i. 5-inch  asbestos- 
covered  pipe.  The  exhaust,  a  2-inch  pipe, 
was  open  to  the  atmosphere. 

Auxiliary  Chemical  Pumps.  —  The  device 
used  for  pumping  the  solution  of  alum  or  sul 
phate  of  alumina  consisted  of  small  plunger 
extensions  of  the  main  piston-rods  on  the 
water  pumps  above  described.  These 
worked  in  pockets  in  which  they  caused  al 
ternate  suction  and  pressure.  The  valve  sys 


tem  was  a  pair  of  cup  valves  in  the  same 
casting,  one  opening  to  allow  flow  from,  and 
the  other  to  allow  flow  into,  the  plunger 
pocket.  These  valves  were  located  just  out 
side  of  the  plunger  chamber. 

Piping  System. — From  the  mixing  tanks  a 
system  of  o.5-inch  brass  pipes  led  to  the  aux 
iliary  pumps.  The  arrangement  was  such 
that  either  tank  could  be  used,  and  either 
one  or  both  of  the  auxiliary  pumps  op 
erated.  From  the  pump  the  solution  of 
chemicals  was  forced  through  a  system  of 
o.75-inch  brass  pipes  into  a  glass  tube.  A  3- 
inch  brass  air-chamber  in  the  system  equal 
ized  the  flow. 

This  glass  tube  was  connected  at  the  bot 
tom  with  a  brass  pipe  which  led  into  the  in 
let  water-pipe,  discharging  in  the  center  of 
the  inlet  pipe  through  a  tee  set  with  its  long 
arm  with  the  current.  The  glass  tube  was 
also  connected  at  the  top  with  the  top  of  a 
6-inch  air-chamber  in  the  inlet  water-pipe. 
A  body  of  air  was  always  maintained  in  this 
chamber,  and  there  was  a  corresponding  ver 
tical  air  column  in  the  glass  tube,  as  the  level 
of  the  chamber  and  of  the  tube  were  the  same. 
By  this  arrangement  the  alum  or  sulphate  of 
alumina  solution  was  discharged  through  an 
air  column,  thus  making  the  flow  of  the  solu 
tion  plainly  visible. 

Manner  of  Control. — As  the  pumps  dis 
charged  a  constant  quantity,  regulation  of  the 
application  of  chemicals  was  obtained  by  re 
lief  pipes  and  valves  through  which  the  excess 
of  solution  was  returned  to  the  mixing  tanks 
and  pumped  over  again. 

Elevations. — The  relative  elevations  in  feet, 
with  the  bottom  of  the  sand  layer  of  the  pres 
sure  filter  as  the  datum  plane,  were  as  follows: 
Maximum  flow  level  in  mixing  tanks.  .  .0.00 
Minimum  flow  level  in  mixing  tanks.  -3.34 

Center  of  pumps -  2.70 

Center  of  discharge  into  inlet +  1.80 

Jcivcll  Device  for  Application  of  Lime. 

The  device  used  for  adding  lime  to  the 
river  water  was  modified  a  number  of  times 
during  its  use.  At  first  it  consisted  simply 
of  an  ordinary  barrel  and  suitable  piping  as 
described  below.  The  barrel  was  located  on 
the  upper  floor.  Unslaked  lime  was  put  in 
the  barrel  and  a  stream  of  water  let  in  at  the 


46 


WATER   PURIFICATION  AT  LOUISVILLE. 


bottom.  The  flow  of  water  into  the  barrel 
was  regulated  by  a  float  valve.  Near  the  top 
of  the  barrel  a  pipe  led  to  a  connection  with 
the  suction  pipe  from  the  sulphate  of  alumina 
tanks.  To  the  lower  end  of  this  pipe  was  at 
tached  a  glass  cylinder  in  order  to  make 
visible  the  rate  of  flow.  The  mixed  milk  of 
lime  and  sulphate  of  alumina  solutions  were 
forced  into  the  main  inlet  water-pipe  by  the 
same  pump.  At  first  the  solution  was  stirred 
by  hand,  but  later  an  aspirator  was  intro 
duced. 

When  the  use  of  lime  was  resumed  on 
March  21  the  milk  of  lime  solution  was 
pumped  through  a  separate  pipe  into  the 
inlet  water-pipe  just  outside  the  settling 
chamber;  and  the  entire  lime  system  was 
independent  of  the  sulphate  of  alumina  sys 
tem. 

Elevations. — The  relative  elevations  in  feet, 
with  the  bottom  of  the  sand  layer  as  the  da 
tum  plane,  were  as  follows: 

Discharge  level  in  the  lime 

barrel +  13.00  (approx.) 

Center  of  modified  dis 
charge  into  inlet  pipe.  .  -  5.95 


The  device  used  for  the  application  of  iron 
consisted  of  a  cast-iron  tank,  approximately 
j  foot  in  diameter  and  3  feet  long,  filled  with 
scrap-iron.  The  piping  was  so  arranged  that 
the  suction  from  the  sulphate  of  alumina 
tanks,  the  suction  from  the  lime  barrel,  and 
the  force  main  from  the  sulphate  of  alumina 
pump  could  be  connected  with  this  tank. 
The  iron  could  be  thus  introduced  at  any 
desired  point  in  the  flow  of  chemicals. 
It  can  hardly  be  said  to  have  been  in  actual 
service,  but  was  tried  on  Feb.  10  and  12,  and 
again  for  2.5  hours  on  Feb.  22.  Its  use  was 
discontinued  on  the  latter  date  on  account  of 
the  very  evident  presence  in  the  effluent  of 
dissolved  iron. 

Jewell  Device  for  the  Application  of  Chlorine. 

This  device  consisted  of  a  set  of  small  U- 
shaped  tubes,  in  which  a  common  salt  solution 
was  decomposed  by  an  electric  current.  A 


constant  flow  of  water  was  maintained 
through  the  tubes.  The  water  dissolved  the 
hypochlorites  and  carried  them  with  it  to  the 
water  in  the  top  of  the  filter.  The  apparatus 
was  never  used  regularly,  but  was  tried  on 
Jan.  21  and  22,  and  for  very  short  periods 
at  later  dates.  On  Jan.  22  available  chlorine 
was  applied  in  this  way  during  the  morning 
at  the  rate  of  o.  i  part  per  million  by  weight 
of  applied  water. 

UNIFORMITY  IN  THE  RATE  OF  APPLICATION 

OF  CHEMICALS  IN  THE  RESPECTIVE 

SYSTEMS. 

Owing  to  the  marked  and  comparatively 
sudden  variations  in  the  quality  of  the  river 
water,  the  rate  of  application  of  chemical  so 
lution  was  varied  by  necessity  from  time  to 
time.  But  with  regard  to  uniformity  when 
the  quality  of  the  river  water  was  practically 
the  same  the  observations  revealed  several 
points  of  an  unsatisfactory  nature.  The 
amount  of  attention  which  was  given  to  the 
devices  for  application  of  chemicals,  further 
more,  was  found  to  be  a  very  important  fac 
tor  in  most  instances. 

Speaking  in  general  terms,  the  application 
of  chemicals  by  the  Warren  device  was  fairly 
satisfactory.  Its  chief  merit  lay  in  the  fact 
that  it  was  automatic.  It  had  a  number  of 
shortcomings,  however.  The  rate  of  appli 
cation  of  chemicals  during  short  periods  was 
variable,  due  to  varying  heights  of  solution 
in  the  pump  box.  When  the  river  water  en 
tered  the  settling  chamber  at  a  rate  of  'ess 
than  about  18  cubic  feet  per  minute  the  pro 
peller  wheel  could  not  be  depended  upon  to 
operate  the  pump  regularly.  So  far  as  was 
learned  the  propeller  was  reasonably  uniform 
in  its  action  when  the  flow  was  greater  than 
that  stated  above.  The  manner  of  regulating 
the  operating  area  of  the  open  arms  of  the 
pump  by  means  of  rubber  stoppers  was  crude, 
and  under  some  circumstances  would  limit 
the  serviceability  of  the  device  in  purifying 
such  a  water  as  that  of  the  Ohio  River. 

The  operations  of  the  Jewell  device  showed 
c1  early  that  its  efficiency  was  closely  depend 
ent  upon  the  attention  which  it  received. 
During  the  latter  part  of  the  test  it  received 


APPLICATION  OF  CHEMICALS    TO    THE  OHIO   RIVER    WATER. 


•17 


sufficient  attention  to  make  its  operation 
satisfactory.  At.  times  during  the  first  part 
of  the  tests,  however,  the  application  of  chem 
icals  was  very  erratic.  In  some  instances  the 
rate  of  application  of  sulphate  of  alumina 
varied  five  or  six  hundred  per  cent,  on  the 
same  day  when  the  quality  of  the  water  was 
about  the  same. 

Complications  arose  when  lime  and  sul 
phate  of  alumina  were  both  applied  by  the 
same  device  in  the  Jewell  System.  At  times 
it  appeared  that  the  two  chemicals  entered 
the  water  alternately. 

With  the  first  Western  device  control  of 
the  application  of  alum  was  repeatedly  lost, 
even  with  a  laborer  spending  the  greater  part 
of  his  time  watching  it.  The  Western  Com 
pany  abandoned  this  device  in  April. 

The  second  Western  device  gave  fairly 
satisfactory  results,  although  it  was  necessary 
to  give  close  attention  both  to  the  stuffing 
boxes  between  the  water  pumps  and  chemical 
pumps,  and  to  the  relief  valves  on  the  pipes 
through  which  the  excess  of  solution  was  re 
turned  to  the  mixing  tanks. 

This  feature  of  the  application  of  chemicals 
is  a  very  important  one,  both  with  regard  to 
the  cost  and  the  efficiency  of  purification,  and 
will  be  discussed  in  Chapter  IX. 

STREN'GTH    OF    SOLUTIONS    OF    CHEMICALS 

APPLIED  TO  THE  RIVER  WATER  IN  THE 

RESPECTIVE  SYSTEMS. 

Samples  of  the  alum  and  sulphate  of  alu 
mina  solutions  used  in  the  several  systems 
were  collected  at  frequent  but  irregular  inter 
vals  for  examination.  The  specific  gravity 
of  the  samples  was  determined  by  the  aid 
of  a  Sartorius  balance,  and  these  readings 
were  converted  into  percentages  of  applied 
chemicals  from  tables  of  factors  which  were 
checked  from  time  to  time.  In  all  1632  de 
terminations  were  made  of  the  strength  of 
applied  chemical  solutions.  In  the  next  set 
of  tables  there  are  given  the  daily  averages 
of  the  percentage  strength  of  the  solutions 
used  in  each  system.  Before  considering 
these  results  there  are  several  comments  to 
be  made. 

In  the  Jewell  System  the  uniformity  of 
strength  of  the  sulphate  of  alumina  solutions 


was  very  satisfactory,  as  a  rule,  during  a 
greater  part  of  the  test.  During  the  first 
portion,  however,  the  variations  in  the 
strength  of  the  solution  were  quite  confus 
ing. 

For  the  most  part  the  uniformity  of 
strength  of  the  sulphate  of  alumina  solutions 
used  in  the  Warren  System  was  fairly  satis 
factory.  Small  variations  in  the  strength  of 
even  consecutive  solutions,  however,  were 
repeatedly  noted.  This  was  due,  apparently, 
to  the  complicated  system  of  preparation  of 
the  solutions,  which  involved  the  considera 
tion  of  certain  quantities  of  solution  in  each 
tank  when  its  use  was  stopped  to  prepare  new 
solutions,  and  to  too  much  dependence  upon 
hydrometer  readings. 

With  the  first  device  used  in  the  Western 
System  the  variations  in  the  strength  of  the 
alum  solutions  were  so  great  that  this  factor 
placed  the  whole  system  at  a  great  disadvan 
tage  at  times,  in  spite  of  the  comparatively 
close  attention  which  it  received. 

This  device,  which  consisted  of  allowing  a 
small  stream  of  river  water  in  the  inlet  pipe 
to  flow  through  a  by-pass  in  which  was  placed 
an  iron  cyclinder  containing  potash  alum, 
showed  marked  weaknesses,  among  which 
were  the  following: 

1.  The  solubility  of  potash  alum  crystals 
varied  with  the  temperature  of  the  river  water 
in  the  alum  tank. 

2.  The  strength  of  the  solution  applied  to 
the  river  water  varied  with  the  period  of  time 
that  the   river  water  remained   in   the   alum 
tank;   that  is,  it  varied  inversely  with  the  rate 
of  application  of  the  alum  solution. 

3.  The  strength  of  the  solution  varied  with 
the  amount  of  potash  alum  crystals  in  the 
tank. 

4.  There  were  no  ready  means  of  knowing 
how   much  alum  was  being  applied  to  the 
water;  and  in  several  instances  the  alum  crys 
tals  in  the  cylinder  became  exhausted,  or  very 
nearly  so. 

On  many  days  the  strength  of  the  solution 
was  quite  uniform,  especially  during  the  latter 
half  of  the  period  when  this  device  was  used, 
and  when,  at  times,  a  small  gas  flame  was 
placed  beneath  the  inlet  pipe  leading  to  the 
alum  tank  to  increase  the  temperature  of  the 
water.  Similar  results  to  the  following  were 


48 


W 'AT 'ER   PURIFICATION  AT  LOUISVILLE. 


frequently  obtained,  however,  during  the  first 
two  months  that  the  system  was  in  operation. 


Date. 

Hour 

Percent 
age  of 
Alum  in 

Date. 

Hour. 

*K?"f 
Alum  in 

1896. 

Applied 
Solution. 

1896. 

Applied 

Jan.  24. 

10.28    A.M. 

7.8 

Feb.  20. 

11.25    A.M. 

3-9 

"•35     " 

5.0 

1.20    J'.M. 

5-7 

11 

12.32      I'.M. 

6.2 

3-  30 

3-3 

" 

1.30        " 

3-2 

4.00 

4-6 

14 

3-"7      ' 

5-1 

4-3° 

5-2 

5.00 

5-2 

5-30 

5-1 

The  following  results,  obtained  on  Feb.  26, 
are  more  representative  of  the  last  portion  of 
the  period  when  more  care  was  taken  to  pre 
vent  the  exhaustion  of  alum  from  the  tank. 


Percentage  of 

Percentage  of 

Hour. 

Alum  in  Applied 

Hour. 

Alum  in  Applied 

Solution. 

Solution. 

9.3O  A.M. 

5-9 

2.30  P.M. 

6.5 

1  1  .  OO      " 

4-9 

3.00 

6.4 

12.30  P.M. 

5-9 

3-3° 

(>.5 

I  .  OO      '  ' 

6.1 

4.00 

5-7 

1.30      " 

6.2 

4.30 

6.6 

2.00      " 

5-9 

5.OO 

6-5 

With  the  second  device  for  the  application 
of  chemicals  in  the  Western  Systems,  there 
came  an  improvement  in  the  uniformity  of  the 
strength  of  solutions,  but  it  was  not  thor- 

DAILY 


oughly  satisfactory.  This  was  due  in  part  to 
mistakes  in  weighing  out  Jhe  alum  or  sul 
phate  of  alumina,  and  in  part  to  accidental 
dilution  of  the  solutions  after  their  prepara 
tion.  An  important  factor  in  these  varying 
strengths  of  solution,  the  effect  of  which  is 
difficult  to  estimate  accurately,  was  the  flow 
of  river  water  from  the  water  pumps  through 
the  stuffing  boxes  into  the  pumps  containing 
the  solution  of  alum  or  sulphate  of  alumina. 

This  was  repeatedly  observed  and  guarded 
against  in  part  by  frequent  packing  of  the 
stuffing  boxes.  The  maximum  leak  noted 
was  about  i  gallon  per  hour  for  one  of  the 
two  pumps.  Under  the  conditions  on  that 
day,  May  20,  the  dilution  from  this  single 
pump  amounted  to  about  10  per  cent,  of  the 
full  quantity  of  solution  in  one  tank  when  full. 
With  more  nearly  normal  rates  of  flow  of 
water  and  of  alum  solution  this  percentage 
would  be  somewhat  less,  but  on  the  other 
hand  the  effect  of  the  dilution  from  this 
source  became  cumulative,  owing  to  the  pas 
sage  through  the  pumps  of  an  excess  of  the 
solution,  and  its  return  through  relief  pipes 
leading  back  to  the  mixing  tanks.  The  last 
portion  of  the  solution  from  the  tank  was 
thereby  more  diluted  than  the  first. 


AVERAGES   OF   THE   PERCENTAGE  STRENGTH    OF   THE   SOLUTIONS  OF   SULPHATE    OF 
ALUMINA    APPLIED    TO   THE    RIVER    WATER    IN    THE   WARREN    SYSTEM. 


l>»y. 

June. 

'  July. 

2.  SO 

JO 

5 

1  .25 

I.  80 

I.  80 

18 

2.  2O 

.60 

2.  IO 

60 

* 

80 

I  .80 

25 

I-  06 

I.  10 

1-90 

2.00 

2.50 

70 

.00 

2.OO 

2.80 

6O 

, 

.60 

APPLICATION  OF  CHEMICALS    TO    THR   OHIO   RIVER    WATER. 


f- 


DAILY    AVERAGES    OF    THE    PERCENTAGE    STRENGTH    OF    THE    SOLUTIONS    OF    SULPHATE    OF 
ALUMINA    APPLIED   TO   THE    RIVER    WATER    IN    THE   JEWELL   SYSTEM. 


Day. 

October. 

November. 

December. 

January. 

February. 

March. 

April. 

May. 

June. 

July. 

o  80 

" 

0.33 

o  60 

6 

o  85 

8 

0.29 

i 

12 

0.34 

0.44 

0.31 

o  85 

0.28 

0.64 

16 

0.30 

0.40 

O.6o 

18 

o  60 

0.30 

0.88 

o  88 

21 

0.24 

0.30 

0.88 

O.6o 

O.2O 

0,65 

I    4O 

0.30 

0.26 

0.80 

0.58 

fin 

26 

0.38 

0.39 

0.80 

O.So 

27 
28 

0-39 

0.80 

o  80 

0.65 

0-45 

.20 

O.6o 

0.60 

0.90 

i.  So 

•?n 

0.95 

0.37 

i  .60 

0.70 

I  .20 

DAILY    AVERAGES    OF    THE    PERCENTAGE    STRENGTH    OF    THE    SOLUTION    OF    ALUM    AND    OF 
SULPHATE   OF    ALUMINA    APPLIED    TO   THE    RIVER    WATER    IN   THE   WESTERN    SYSTEMS. 


Day. 

January.* 

February. 

March. 

April. 

May. 

June. 

July. 

I 

6.0 

6.7 

2    6 

8  o 

3 

6.0 

3  8 

5  8 

5 

6    2 

6 

6   I 

7 

-j   s 

8 

6  6 

10 

5.2 

6  7 

it 

6  0 

2   3 

2    6 

o  8 

2    6 

13 

6   2 

6  9 

14 

4-3 

6.0 

6  8 

15 

6.8 

4.2 

2.2 

2.9 

16 

7.2 

17 

5.8 

4-6 

6.6 

2.2 

2.O 

18 

5.8 

6  5 

1.8 

19 

6  8 

20 

5  (> 

2.8 

21 

5.8 

(,  3 

22 

5  -2 

o  6 

23 

5.6 

o  6 

24 

5  -5 

5.6 

25 

4.0 

5-4 

6.0 

0.6 

2.  I 

26 

6  i 

6    Q 

o  8 

27 

6.0 

6  o 

28 

5.2 

6.9 

2g 

6  8 

30 

2  6 

2    6 

31 

5.8 

7-  1 

2.0 

*  The  meter  on  the  alum  pipe  was  not  attached  till  Jan.  10;  and  from  Dec.  23  to  that  time  ihe  amount  of  alum  applied 
to  the  water  was  computed  from  the  weight  of  alum  put  into  the  alum  tank. 


WATER   PURIFICATION  AT  LOUISVILLE. 


AVERAGE  DAILY  AMOUNTS,  IN  GRAINS  PER 
GALLON,  OF  SULPHATE  OF  ALUMINA 
APPLIED  TO  THE  OHIO  RlVER  WATER 
IN  THE  RESPECTIVE  SYSTEMS. 

The  daily  average  results  of  the  determina 
tion  of  the  amounts  of  sulphate  of  alumina 
used  in  the  respective  systems  (from  October, 
1895,  to  July,  1896,  inclusive)  are  presented 
in  the  following-  tables.  In  the  case  of  the 
Western  Systems,  when  both  niters  were  in 


operation,  the  average  results  refer  to  the 
filters  in  common. 

As  already  explained  alum  was  used  during 
a  large  portion  of  the  time  in  the  Western 
Systems,  and  in  all  cases  it  is  converted  into 
equivalent  amounts  of  sulphate  of  alumina. 

As  a  matter  of  convenience  these  results 
are  expressed  in  grains  per  gallon.  They 
may  be  changed  to  parts  per  million  by  mul 
tiplying  by  17.1,  and  to  pounds  per  million 
gallons  by  multiplying  by  143. 


AVERAGE    DAILY    AMOUNTS,   IN   GRAINS    PER   GALLON,  OF  SULPHATE  OF   ALUMINA  APPLIED  TO 
THE   OHIO   RIVER   WATER    IN  THE   WARREN    SYSTEM. 


Day. 

October. 

November. 

December. 

January. 

February. 

March. 

April. 

May. 

June. 

July. 

0.88 

6.  53 

I.l6 

4.05 

3.82 

o  78 

5  85 

5-  '9 

5.03 

•3    eg 

5  89 

i  66 

4   18 

I    85 

3.27 

6 

o  68 

3  86 

1.83 

3-  12 

3.36 

3  56 

i   86 

I    28 

8 

4  46 

2.88 

i.  08 

3.87 

1.89 

1  .  59 

4.78 

2.73 

2    85 

i   88 

4.00 

3-  29 

2.32 

2.40 

3.04 

I   67 

o  18 

4  83 

i  81 

1.78 

3.18 

c   76 

i   66 

3  28 

2.87 

16 

4  48 

i   89 

2.68 

2.83 

18 

o  88 

3  61 

2.32 

2.76 

20 

2.88 

1.58 

i  .15 

2.65 

2.80 

•j  82 

o  83 

o  85 

1.68 

4.33 

i   58 

6  37 

3.64 

2.  15 

6.45 

i   36 

o  84 

7.41 

0.66 

2.38 

7.40 

26 

T     6.1 

A   6c 

i   28 

28 

3  60 

1  58 

o  87 

5.16 

4.84 

3-95 

4.42 

4  08 

5   78 

4.  17 

APPLICATION  OF  CHEMICALS    TO    THE   OHIO   RIVER    WATER.  51 

AVERAGE   DAILY   AMOUNTS,   IN   GRAINS   PER  GALLON.  OF   SULPHATE   OF   ALUMINA  APPLIED  TO 
THE    OHIO    RIVER   WATER    IN    THE   JEWELL   SYSTEM. 


Day. 

October. 

November. 

December. 

January. 

February. 

March. 

April 

May. 

Tune. 

July. 

l 

4  68 

o  80 

5.87 

6    71 

2    82 

i  .  13 

4-55 

5-94 

6.33 

4.16 

1.62 

4.31 

"    64 

I    69 

5  06 

6 

3.56 

0.98 

4.05 

1.65 

4.35 

4.67 

o  88 

i   18 

I     64 

8 

2  68 

i   6r 

6.36 

o  81 

i  .30 

1.61 

5.  go 

6.17 

2    08 

2.18 

O    qq 

i  61 

i   62 

o  58 

.38 

1.64 

3.  Si 

6.36 

i    38 

o  85 

i   61 

15 

2.8l 

.31 

5.78 

1  6 

i   28 

i   62 

5   64 

2    48 

4   82 

18 

i  60 

5   Si 



3  08 

2    85 

o  86 

i  68 

i   83 

o  89 

.25 

I  .93 

8.32 

25 

I   66 

0.98 

1.65 

10.83 

26 

o  84 

i   08 

•i  8-} 

27 

i   65 

1.48 

8  75 

28 

.36 

3  38 

6  95 

29 

2.06 

4   ^3 

6.24 

7.58 

3° 

0.41 

4   3S 

4.85 

8.72 

AVERAGE   DAILY    AMOUNTS,   IN    GRAINS    PER   GALLON,    OF   SULPHATE   OF    ALUMINA    APPLIED 
TO   THE   OHIO    RIVER   WATER    IN    THE    WESTERN    SYSTEMS. 


Day. 

January. 

February. 

March. 

April. 

May. 

June. 

July. 

4  38 

4  87 

o  63 

2    83 

2    64 

6 

0.82 

3   16 

4.28 

S    <>2 

8 

4.61 

O.8O 

6.32 

o  66 

3-  16 

II 

o  62 

5-77 

1.48 

5-S6 

I       06 

o  83 

4-84 

15 

5-  10 

16 

i   66 

4.18 

•S      -36 

18 

I  .24 

0.84 

O.5I 

i  .52 

3.66 

20 

i  .24 

2.78 

0.83 

5.39 

3.70 

o  87 

22 

1.58 

3-29 

4.46 

23 

3.83 

7.08 

24 

0.81 

1.36 

4.56 

3.64 

8.31 

25 

I    63 

5.20 

26 

3  78 

27 

i   58 

r   16 

2    87 

5.38 

28 

2.60 

5.36 

29 

6  18 

6  98 

6   71 

11 

3.83 

2  WATER   PURIFICATION  AT  LOUISVILLE. 

AMOUNTS  OF  LIME  USED  IN  THE  JEWELL  SYSTEM. 
DAILY  AVERAGES  OF  PERCENTAGE  STRENGTHS  OF  LIME  SOLUTION  USED  IN  THE  JEWELL 

SYSTEM. 


Date. 

1896. 

Strength. 

Date. 

1896. 

Strength. 

Date. 
1896. 

Strength. 

Date. 
1896. 

Street!,. 

February     8 

0.52 

February   18 

0.55 

February  27 

0.49 

March     7 

0.44 

"           10 

o.  52 

19 

0-55 

28 

0.49 

"         21 

o.  19 

"           II 

0.52 

"           20 

0.49 

29 

0-53 

"         23 

0.30 

"              12 

0.52 

21 

0.49 

March        2 

0.44 

"       25 

0.40 

13 

o-55 

"             22 

0.49 

3 

0.44 

26 

0.25 

14 

0.55 

24 

0.49 

4 

0.44 

"     27 

0.21 

15 

o-55 

25 

o.  52 

"                 *, 

0.44 

31 

0.25 

i? 

0-55 

26 

0.52 

6 

0.44 

April        i 

0.30 

The  daily  average  results  of  the  amounts    of  lime  used  in  the  Jewell  System  are  pre 
sented  in  the  following  table: 

AVERAGE    DAILY    AMOUNTS,    IN   GRAINS    PER    GALLON,   OF    LIME    APPLIED   TO   THE   OHIO    RIVER 

WATER    IN    THE   JEWELL   SYSTEM. 


Date. 

1896. 

Amount. 

Date. 
1896. 

Amount. 

Date. 

1896. 

Amount. 

Date. 
1896. 

Amount. 

February    8 

0.85 

February  18 

1.05 

February  27 

0.32 

March      7 

0.23 

"              10 

I.38 

19 

1.17 

28 

0.03 

'•          21 

0.28 

II 

1.67 

20 

0.88 

29 

o.i  8 

23 

0.72 

"               12 

1.56 

"             21 

0.47 

March    2 

0.19 

25 

0.49 

13 

0.52 

"               22 

0.32 

3 

0.17 

26 

1.05 

H 

0.72 

24 

0.46 

4 

0.19 

27 

1.41 

15 

0.92 

25 

0.38 

5 

0.18 

31 

2.17 

17 

0.82 

"        '       26 

o.53 

"          " 

0,3 

April  i 

o.S  I 

DECOMPOSITION  AND   SUBSEQUENT  DISPOSAL    OF   THE  ALUM. 


53 


CHAPTER   ill. 


DECOMPOSITION  AND  SUBSEQUENT  DISPOSAL   OF  THE  ALUM  OR  SULPHATE  OF  ALUMINA 
APPLIED  TO  THE  OlIIO  RlVER  WATER. 


IN  some  localities  objections  have  been 
raised  to  the  use  of  alum  and  of  sulphate  of 
alumina  in  the  purification  of  public  water 
supplies.  The  ground  for  this  has  been  that 
some  of  the  dissolved  chemicals  passed 
through  the  filter,  appeared  in  the  filtered 
water,  and  were  liable  to  injure  the  health  of 
the  water  c6nsumers.  While  this  might  be 
true  with  some  waters,  it  can  be  positively 
stated  that  it  should  not,  and  need  not,  be  the 
case  with  the  Ohio  River  water  at  Louisville. 
The  reasons  for  this  are  that  there  is  dissolved 
in  the  Ohio  River  water  an  ample  supply  of 
lime  and  magnesia  to  combine  with,  and  to 
decompose,  more  sulphate  of  alumina  than 
would  be  necessary  to  apply  under  conditions 
giving  a  satisfactory  and  economical  purifi 
cation  of  the  water  by  the  general  method 
under  consideration. 

The  lime  and  magnesia  which  are  found  in 
the  river  water,  in  a  form  capable  of  decom 
posing  sulphate  of  alumina,  are  present  as 
carbonates  and  bicarbonates.  In  the  tables 
of  chemical  analyses  of  the  river  water  in 
Chapter  I  the  amounts  of  these  constituents 
are  recorded  as  alkalinity.  These  compounds 
which  give  to  the  water  its  alkalinity  possess 
the  power  of  decomposing  sulphate  of  alumina 
and  alum,  by  virtue  of  the  fact  that  the  sul 
phuric  acid  of  the  applied  chemicals  is  much 
stronger  than  the  carbonic  acid  of  the  alkaline 
compounds.  The  result  is  that  the  sulphuric 
acid  (the  strong  acid)  combines  with  the  lime 
or  magnesia  (the  strong  bases);  the  alumina  is 
thus  disengaged  and,  in  the  presence  of  the 
water,  forms  aluminum  hydrate,  which  soon 
appears  in  the  form  of  a  white  gelatinous  solid 
compound;  and  the  carbonic  acid  (the  weak 
acid)  remains  in  the  water  as  free  acid.  Tak 
ing  sulphate  of  alumina,  the  more  efficient  of 
the  two  chemicals,  as  an  example,  and  view 


ing  the  results  of  its  application  to  the  Ohio 
River  water  in  the  light  of  the  expressions 
used  in  water  analysis,  we  find  that  the  follow 
ing  principal  changes  occur: 

1.  The  alkalinity  is  reduced  by  the  displace 
ment    of    carbonic    acid    by    sulphuric    acid, 
which,   combining   with   the   lime  and   mag 
nesia,  forms  neutral  sulphates. 

2.  The    alumina    is    freed    from    sulphuric 
acid  when  the  latter  unites  with  the  alkaline 
constituents,  and  appears  as  the  gelatinous, 
solid  aluminum  hydrate,  which  possesses  the 
power  of  coagulating  the  suspended  matters 
in  the  water.     In  its  solid  form  the  aluminum 
hydrate  is  removed  subsequently  by  sedimen 
tation  and  filtration. 

3.  The     incrusting     constituents     arc     in 
creased,   due   to   the   sulphuric   acid   uniting 
with  the  lime  and  magnesia. 

4.  The  free  carbonic  acid  is  increased  on 
account  of  the  liberation  of  this  acid  when  the 
alkalinity  is  reduced,  with  a  resulting  increase 
in   the    incrusting   constituents.     At   the   in 
stant  of  liberation  it  exists  as  a  gas,  but  it  im 
mediately  takes  up  water  and  forms  free  car 
bonic  acid. 

It  is  noted  above  that  these  are  the  principal 
changes.  If  the  river  contained  no  suspended 
matter  or  dissolved  organic  matter,  there 
would  be  no  other  action;  and  these  changes, 
furthermore,  would  be  proportional  to  the 
amount  and  composition  of  the  applied  sul 
phate  of  alumina.  In  practice  it  is  found  that 
the  particles  of  suspended  matter,  by  an  ab 
sorptive  or  mordanting  action,  dispose  of 
some  of  the  sulphate  of  alumina,  without  the 
above  decomposition  taking  place.  This 
secondary  action  will  be  mentioned  be 
yond. 

Considering  the  primary  decomposition 
(in  a  water  free  from  suspended  matters  and 


54 


WATER   PURIFICATION  AT  LOUISVILLE. 


dissolved  organic  matter),  the  reduction  in 
alkalinity  in  parts  per  million,  for  i  grain  per 
gallon  of  each  lot  of  the  chemicals  used  in 
these  tests,  would  be  proportional  to  the  sul 
phuric  acid,  as  follows: 

REDUCTION  OF  ALKALINITY  (LIME  AND  MAG 
NESIA)  BY  ONE  GR<UN  PER  GALLON  OF 
EACH  LOT  OF  COMMERCIAL  SULPHATE 
OF  ALUMINA. 


System. 

Number  of 

Percentage  of 
Sulphuric  Acid. 

Reduction  in 
Alka  inity. 
Parts  per  Million. 

Warren 

I 

39-87 

8-53 

2 

38.61 

8.27 

3 

37-72 

8.07 

Jewell 

I 

37.96 

8.12 

2 

37-87 

8.  II 

3                     37-46 

8.02 

4 

42.  2O 

9.04 

Western 

i 

37-72 

8.07 

2 

37.64 

8.06 

Under  the  above-mentioned  conditions,  the 
increase  in  incrusting  constituents,  expressed 
in  the  usual  way  in  parts  per  million,  would 
be  exactly  proportional  to  the  reduction  in 
alkalinity;  and  the  increase  in  carbonic  acid, 
expressed  in  parts  per  million  by  weight  of 
carbon  dioxide,  would  be  44  per  cent,  of  the 
reduction  in  alkalinity. 

Independent  of  the  absorptive  and  mor 
danting  action  with  suspended  matters  and 
certain  dissolved  organic  matters,  the  changes 
in  the  river  water,  upon  the  addition  of  I 
grain  per  gallon  of  the  first  lot  of  sulphate  of 
alumina  used  with  the  Warren  System,  may 
be  illustrated  as  follows: 

COMPARISON  IN  PARTS  PER  MILLION  OF 
IMPORTANT  CONSTITUENTS  OF  THE  OHIO 
RIVER  WATER  BEFORE  AND  AFTER  TREAT 
MENT  WITH  ONE  GRAIN  PER  GALLON  OF 
SULPHATE  OF  ALUMINA. 
Befor< 


Alkalinity 

Incrusting    constituents... 

Carbonic       acid       (carbon 

dioxide) 


After  Treatment. 

51.47 (decrease) 
33.53  (increase) 

63.75  (increase) 

When  suspended  matter,  especially  clay,  is 
present  in  the  water,  there  is  a  certain  amount 
of  the  sulphate  of  alumina  absorbed  without 
its  decomposition  by  the  alkaline  constitu 
ents.  This  causes  the  alkalinity  to  be  reduced 
in  amounts  less  than  that  indicated  above. 
The  degree  of  reduction,  furthermore,  varies 
with  the  amount  and  character  of  the  matter 


in  suspension.  The  Ohio  River  contains  so 
little  dissolved  organic  matter  that  this  factor 
probably  does  not  cause  the  actual  reduction 
in  alkalinity  to  depart  from  the  theoretical 
more  than  about  5  per  cent.  But  the  varying 
composition  of  the  Ohio  River  water,  with  re 
gard  to  suspended  matter,  causes  a  variable 
relation  to  exist  between  the  theoretical  re 
duction  in  alkalinity,  due  to  complete  decom 
position  of  the  applied  sulphate,  and  the 
actual  reduction  after  a  portion  of  it  has  been 
absorbed  by  the  suspended  matter.  The 
significance  of  this  is  shown  in  the  following 
table,  where  the  average  results  of  several  de 
terminations  are  presented,  in  which  the 
amount  of  sulphate  of  alumina  was  sufficient 
to  produce  complete  coagulation. 

PERCENTAGES  WHICH  THE  ACTUAL  REDUC 
TION  OF  ALKALINITY  BY  SULPHATE  OF 
ALUMINA  WERE  OF  THE  THEORETICAL, 
WITH  OHIO  RIVER  WATER  CONTAINING 
AMOUNTS  OF  SUSPENDED 


D  IFF  ERF.  NT 
MATTER. 


200 
400 


vhich  the  Actual 


Further  information  upon  this  point  was 
obtained  in  1897,  and  the  results  are  recorded 
in  Chapter  XV. 

Combining  the  above  information  con 
cerning  the  decomposition  of  sulphate  of  alu 
mina  with  the  varying  amounts  of  alkalinity 
in  the  river  water,  as  recorded  in  Chapter  I, 
it  will  be  seen  that  the  greatest  amount  of 
sulphate  of  alumina  which  can  be  safely  ap 
plied  to  the  ( )hio  River  water  is  about  4 
grains  per  gallon  for  a  minimum;  the  normal 
ranges  from  (>  to  10  grains;  and  the  maxi 
mum  about  15  grains  per  gallon. 

From  the  outset  of  these  investigations,  the 
importance  of  determining  accurately  the 
presence  or  absence  of  the  applied  alum  or 
sulphate  of  alumina  in  the  filtered  water  was 
clearly  recognized.  There  are  two  methods 
which  can  be  utilized  in  the  solution  of  this 
problem.  These  methods,  both  of  which  were 
carefully  applied  to  samples  of  the  filtered 
water  day  by  day,  are  as  follows: 

i.  The  determination  of  the  alkalinity  of 
the  effluents.  This  proved,  if  the  effluents 


DECOMPOSITION  AND   SUBSEQUENT  DISPOSAL    OF    THE  ALUM. 


55 


were  alkaline,  that  no  undecomposed  sulphate 
of  alumina  was  present.  If  the  effluent  was 
acid,  however,  the  opposite  of  this  was  true. 

2.  The  test  for  alumina  in  the  effluent,  ac 
cording  to  Richards'  logwood  and  acetic 
acid  test. 

In  the  following  table  are  presented  all  re 
sults  in  which  any  trace  of  alumina  (A12O3) 
was  found  in  the  filtered  water,  together 
with  the  corresponding  alkalinity  or  acidity 


of  each  sample.  The  amount  of  sulphate  of 
alumina  equivalent  to  each  amount  of 
alumina  is  also  recorded.  It  will  be  noted, 
in  those  cases  where  the  effluents  were  acid, 
that  the  amounts  of  alumina  and  sulphate  of 
alumina  were  abnormally  low.  This  may  have 
been  due  to  changes  in  the  sulphate  of  alu 
mina  in  passing  through  the  filter,  or  to  in 
accuracies  of  the  logwood  test  in  measuring 
such  small  quantities  of  alumina,  or  both. 


SUMMARY   OF   ALL   RESULTS   SHOWING   ALUMINA    BY   THE    LOGWOOD    AND    ACETIC   ACID  TEST, 
WITH    THE   CORRESPONDING   ALKALINITY    IN    THE    EFFLUENT   OF   EACH    SYSTEM. 


Date. 
.896. 

Alkalinity. 
Parts  per  Million. 

Parti  per  Mil'lion. 

Sulphate  of 

Grains  per 
Gallon. 

Date. 

1896. 

Alkalinity. 
Parts  per  Million. 

Pam'per 
Million. 

Sulphate  of 
Grains  per 

rn.       .11. 

JEWELL  EFFLUENT. 

February  15 

"             20 

6.5 

17.0 

O.2 
0.  I 

0.07 
0.04 

March       27 

59-2 

0.  I 

0.04 

March        16 

12.0 

O.  I 

0.04 

"            28 

31-9 

O.  I 

0.04 

"                 20 

I3.I 

O.I 

0.04 

April           2 

5-5 

0.3 

0.17 

"                 21 

IO.  I 

O.  I 

0.04 

3 

1-3 

0.2 

0.07 

23 

4-9 

O.  I 

0.04 

4 

Acidity  4.7 

0.7 

0.25 

24 

4.0 

O.  I 

0.04 

6 

4.0 

0.2 

0.07 

April            2 

0.2 

0.5 

0.18 

June            2 

28.9 

O.  I 

0.04 

3 

Acidity  o.i 

0.3 

O.  I  I 

3 

39-7 

0.  I 

0.04 

6 

Acidity  3.1 

0.8 

0.27 

10 

22.5 

0.3 

O.II 

"               7 

3-5 

0.5 

o.iS 

16 

24.0 

O.I 

0.04 

July             3 

10.2 

o.  r 

0.04 

July             I 

Acidity  1.8 

o-3 

O.  1  I 

2 

Acidity  3.9 

0.4 

0.13 

WKSTKK.N     r.KAVlTY     EM-  LU  K.VI'. 

3 

4.6 

o.S 

0.27 

July             2  ;             6.1 

O.2 

0.07 

8 

8.8 

O.  I 

0.04 

"                 3 

6.0 

O.  I 

0.04 

13 

4-1 

0.3 

O.  II 

M 

Acidity  i.o 

0.3 

O.II 

WESTERN    PRKSSURK    EFFLUENT. 

15 

2-5 

O.2 

0.07 

April  3                     3.0 

O.2 

0.07 

17 

IO.O 

0.4 

0.13 

"     4 

Acidity  i.o 

0.4 

0.13 

20 

15.2 

O.2 

0.07 

"     6 

5.0 

0.2 

0.07 

21 

17.1 

O.I 

0.04 

22 

14.0 

O.  I 

0.04 

JEWELL  EFFLUENT. 

23 

8.9 

o.i                 0.04 

February  10               43  -o 

O.2 

0.07 

24 

Acidity  2.1 

0.3                   o.i  I 

"          20               14.9 

0.2 

0.07 

25 

Acidity  6.0 

0.3                  o.ii 

March       24 

15-4 

O.  I 

0.04 

27 

Acioity  3.8 

0.3                  o.ii 

26 

51.1 

0.  1 

0.04 

28 

Ai-i'iny    l.i) 

0.2                      0.07 

The  above  results  show  that  on  2,  8,  o,  and 
i  days,  respectively,  the  Warren,  Jewell, 
Western  Gravity,  and  Western  Pressure 
effluents  were  acid,  and  contained,  therefore, 
undecomposed  sulphate  of  alumina.  The 
acidity  on  these  several  occasions  was  due, 
of  course,  to  the  application  of  sulphate  of 
alumina  in  amounts  exceeding  that  capable 
of  decomposition  by  the  alkaline  constituents 
of  the  river  water.  On  a  practical  basis  of 
operation,  such  applications  would  be  inex 
cusable. 

It  will  also  be  noted  from  the  results  in  the 
last  table  that  on  10,  22,  2,  and  2  days,  respec 
tively,  the  Warren,  Jewell,  Western  Gravity, 


and  Western  Pressure  effluents  contained 
slight  traces  of  alumina,  although  the  efflu 
ents  were  alkaline.  In  a  majority  of  these 
cases  the  effluents  were  sufficiently  alkaline 
to  decompose  several  grains  of  sulphate  of 
alumina,  and  the  passage  of  the  latter  through 
the  filter  in  an  undecomposed  form,  under 
these  conditions,  was  an  impossibility.  So  far 
as  we  could  learn,  these  slight  traces  of  alu 
mina  in  alkaline  effluents  were  due  to  the 
passage  through  the  filter  of  minute  flakes  of 
the  insoluble  aluminum  hydrate,  and  to  their 
subsequent  solution  by  the  reagents  used  in 
the  logwood  and  acetic  acid  test.  So  far  as 
their  direct  and  inherent  influence  is  con- 


WATER   PURIFICATION  AT  LOUISVILLE. 


cerned,  these  slight  traces  of  alumina  in  an 
alkaline  effluent  cannot  be  regarded  as  objec 
tionable. 

In  conclusion  it  may  be  stated  that  the 
experience  obtained  during  these  tests  shows 
clearly  that  the  Ohio  River  water  contains  a 
sufficient  amount  of  alkaline  compounds  to 
decompose  adequate  quantities  of  sulphate  of 
alumina;  that  the  alumina  appears  as  a  solid 
gelatinous  body,  which  coagulates  the  mud 
silt  and  clay,  and  subsequently  is  completely 
removed,  practically  speaking,  by  sedimenta 
tion  and  nitration;  and  that  the  sulphuric  acid 
combines  with  lime  and  magnesia  to  form 


neutral  sulphates  of  those  bases,  while  an 
equivalent  amount  of  carbonic  acid  is  formed, 
and  remains  dissolved  in  the  water.  In  a  very 
few  instances  very  slight  amounts  of  unde- 
composed  sulphate  of  alumina  were  found  in 
the  effluent  of  these  systems.  This  was  due 
to  faults  of  construction  of  the  systems,  and 
of  their  operation,  which  must  be  improved 
as  explained  in  Chapters  IX  and  XV. 

Under  the  conditions  of  efficient  and  eco 
nomical  purification  of  this  water,  the  pres 
ence  of  undecomposed  sulphate  of  alumina  in 
the  filtered  water  would  be  not  only  inadmis 
sible,  but  inexcusable. 


COAGULATION  AND   SEDIMKNTA  TION  BY  ALUM1N  UM»  HYDRATE.         57 


(II  XI'TKK    [V. 


COAGULATION  AND  SEDIMENTATION  OF  OHIO    RIVER  WATER  HY  ALUMINUM  HYDRATE 
FORMED  BY  THE  DECOMPOSITION    OF  THE  APPLIED  ALUM  OR 
SULPHATE  OF  ALUMINA. 


IT  has  been  already  shown  in  the  preced 
ing  chapters  how  the  geiaunous  precipitate 
of  aluminum  hydrate  is  lormed,  and  reference 
has  also  been  made  to  the  disposal  of  the 
alumina  in  this  solid  form  by  subsidence  and 
filtration  through  sand.  In  this  chapter  it  is 
the  purpose  to  explain  the  nature  of  coagula 
tion  and  sedimentation,  to  describe  the  de 
vices  in  the  several  systems  where  the  coagu 
lation  and  sedimentation  were  accomplished, 
and  to  point  out  the  practical  results  which 
may  be  obtained  by  the  aid  of  aluminum 
hydrate  in  the  purification  of  such  water  as 
that  of  the  Ohio  River.  Coagulation  is  the 
term  generally  used  to  express  the  action 
which  is  produced  by  the  application  of  alum 
to  water.  In  general  terms  this  action  has  al 
ready  been  described,  but  in  detail  it  is  as  fol 
lows: 

When  the  applied  alum  solution  comes  in 
contact  with  the  dissolved  lime  and  magnesia 
in  the  river  water,  the  former  is  immediately 
decomposed  by  the  latter,  which  are  present 
in  excess.  At  the  instant  of  the  decomposi 
tion  of  the  alum  it  forms  aluminum  hydrate. 
The  latter  is  also  dissolved  in  the  water  at  the 
time  when  the  decomposition  or  reaction 
takes  place.  The  great  bulk  of  aluminum  hy 
drate  passes  very  quickly  into  the  form  of 
solid  matter.  To  chemists  a  solid  compound, 
separating  out  by  the  action  on  each  other  of 
two  soluble  chemical  compounds,  is  known 
as  a  precipitate.  At  first  this  precipitate  of 
aluminum  hydrate  is  present  as  innumerable, 
minute,  white  particles  of  a  gelatinous  and 
sticky  nature;  and  it  is  not  until  the  alum  has 
been  decomposed  and  converted  into  this 
form  that  its  application  in  the  purification, 
by  this* system,  of  such  water  as  that  of  the 
Ohio  River  begins  to  be  of  practical  value, 


by  its  accomplishment  of  the  initial  step  in 
the  purification,  viz.: 

COAGULATION. 

The  process  of  coagulation  consists  of  a 
gradual  grouping  together  of  the  tiny  parti- 
cies  of  aluminum  hydrate  which  surround, 
and  at  the  same  time  envelope,  the  mineral 
matter,  organic  matter,  bacteria,  and  other 
organisms  suspended  in  the  river  water. 
Aluminum  hydrate  (or,  perhaps,  sulphate  of 
alumina)  also  combines  with  some  of  the  dis 
solved  organic  matters,  and  adds  them  to  the 
mass  of  coagulated  material.  Coagulation  of 
muddy  water  by  aluminum  hydrate  may  be 
more  easily  understood  by  comparing  it  to 
the  clarification  of  turbid  coffee  to  which  the 
white  of  eggs  has  been  added. 

The  completeness  with  which  coagulation 
takes  place  depends  upon  the  relation  of  sev 
eral  factors.  But  it  may  be  stated  that,  disre 
garding  the  question  of  cost,  it  is  possible 
with  sufficient  coagulation  followed  by  suf 
ficient  sedimentation  to  render  very  muddy 
water  perfectly  clear.  In  actual  practice  the 
economical  aspects  must  be  considered,  and 
coagulation  should  be  carried  to  such  a  de 
gree,  and  under  such  conditions,  that  sedi 
mentation  will  remove  the  most  mud  and 
other  suspended  matter  for  the  least  money. 
For  efficient  and  economical  filtration  through 
sand  at  a  rapid  rate,"  attention  must  be  given 
also  to  the  coagulated  masses  in  the  water 
as  it  reaches  the  filter. 

The  degree  of  coagulation  is  influenced 
and  controlled  by  several  factors.  Primarily 
it  is  controlled  by  the  amount  of  alum  which 
is  applied  and  decomposed  into  aluminum  hy 
drate.  It  is  also  influenced,  among  other 


.    WATER  PURIFICATION  AT  LOUISVILLE. 


things,  to  a  marked  degree  by  the  amount 
of  suspended  matter  in  the  river  water,  the 
relative  character  of  the  suspended  particles, 
and  the  period  during  which  coagulation  and 
subsequent  sedimentation  may  take  place. 
The  last  factor  is  of  great  economical  im 
portance. 

Coagulation  by  itself  effects  no  purification 
in  the  sense  that  it  removes  from  the  water 
any  objectionable  matters.  it  is  simply  an 
initial  and  very  important  step  in  the  purifi 
cation  of  waters  heavily  charged  with  sus 
pended  matters,  by  which  the  way  is  paved  for 
economical  and  efficient  purification  by  means 
of  sedimentation  and  filtration  through  sand. 

SEDIMENTATION. 

Sedimentation  consists  solely  of  the  sub 
sidence  due  to  gravity  of  the  suspended  mat 
ters  after  coagulation.  It  is  a  process  of 
purification  in  that  it  removes  from  the  water 
objectionable  matters.  It  occurs  in  part 
simultaneously  with  coagulation  in  these  sys 
tems,  but  the  greater  part  of  the  sedimenta 
tion  follows  coagulation. 

In  the  following  pages  are  described  the 
portions  of  each  system  where  the  coagula 
tion  and  sedimentation  took  place.  lieyond 
this  are  given  some  results  showing  the  puri 
fication  effected  by  the  coagulation  and  sedi 
mentation  in  the  respective  systems,  and  an 
account  of  the  relative  value  of  the  above- 
named  factors,  together  with  the  results  of 
some  special  experiments  made  with  the  view 
to  demonstrating  more  clearly  the  economi 
cal  significance  of  these  portions  of  this 
method  of  purifying  the  Ohio  River  water. 

These  descriptions  will  be  more  clearly  un 
derstood  by  reference  to  the  accompanying 
plates. 

WARREN  SETTLING  BASIN. 

The  settling  basin  was  rectangular  in  plan, 
1 2. i  feet  by  12.0  feet,  and  10.25  feet  deep. 
It  was  constructed  entirely  of  yellow  pine. 
The  bottom  was  made  of  planks  2.5  inches 
thick,  and  the  sides  for  a  distance  of  5.1  feet 
above  the  bottom  were  2.5  inches  thick;  above 
this  height  they  were  5  inches  thick.  The 
basin  was  strongly  braced  inside  and  out  by 


white-pine  posts  (6  by  8  inches),  and  the 
foundation  was  made  of  timbers  of  the  same 
size.  Iron  rods  0.375  inch  in  diameter  ex 
tended  across  the  basin  to  stay  it.  Two  par 
titions  or  baffle-walls  divided  the  basin  into 
three  sections  as  shown  on  the  plan.  These 
walls  did  not  extend  entirely  across  the  basin, 
but  left  an  opening  at -one  end  of  2.67  feet. 

These  partitions  were  made  of  i-inch 
sheathing  fastened  to  1.75  by  6-inch  posts. 
The  general  arrangement  of  the  basin  is 
shown  on  the  plans,  as  are  also  the  locations 
of  the  inlet  and  outlet  water-pipes. 

Inlet  Water-pipe. — The  river  water  entered 
the  basin  through  a  6-inch  pipe,  connecting- 
just  inside  the  basin  wall  with  a  6-inch  bal 
anced  valve  controlled  by  a  float.  There  was 
from  45  to  65  pounds  pressure  on  the  inlet 
water-pipe,  which  branched  from  the  force 
main  leading  to  the  Crescent  Hill  Reservoir. 
A  small  propeller-wheel  located  in  a  6-inch 
nipple,  which  extended  5  inches  from  the 
valve,  drove  the  chemical  pump  as  previously 
described. 

Outlet. — The  outlet  was  a  box  channel,  3.4 
by  i.i  feet  in  section.  Its  crest  was  8.7  feet 
above  the  floor  of  the  basin. 

From  the  basin  outlet  an  8-inch  cast-iron 
pipe  led  to  the  filter,  where  it  connected  with 
an  8-inch  pipe,  which  in  turn  connected  with 
the  central  well.  The  passage  of  water  from 
the  basin  to  the  filter  was  controlled  by  an 
8-inch  valve  in  this  pipe. 

Elevations. — The  relative  elevations  in  feet, 
with  the  bottom  of  the  sand  layer  as  the  da 
tum  plane,  were  as  follows: 

Center  of  inlet  water-pipe  at  basin.  .  .  +  1.02 

Floor  of  basin -  1.98 

Top  of  basin +8.52 

Average  maximum  water  level +  8.02 

Crest  of  outlet  (mudsill) +  6.72 

Center  of  pipe  leading  to  the  filter.  .  .  .  +  1.60 

Depth. — The  depths  of  the  chamber  in  feet 
were  as  follows: 

At  level  of  mudsill 8.7 

Average  maximum  water  level 10.0 

Total  depth  of  chamber 10.5 

Area. — The  areas  of  the  chamber  in  square 
feet  were  as  follows: 


COAGULATION  AND   SEDIMENTATION  BY  ALUMINUM  HYDRATE. 


59 


At  floor  level 139-7 

At  level  of  mudsill H3-6 

At  average  maximum  water  level '47-9 

Capacity. — The  capacities  of  the  chamber 
in  cubic  feet  were  as  follows: 

Below  level  of  mudsill 1229 

Below  average  maximum  level  of  water.   1422 
Total  capacity !459 

These  do  not  include  the  outlet  channel, 
the  contents  of  which  were  33.9  cubic  feet. 

Storage  Period. — Assuming  complete  dis 
placement,  the  length  of  time  required  for 
water  to  pass  through  the  basin  at  the  con 
tract  rate  (250,000  gallons  per  24  hours)  was 
61  minutes.  The  distance  from  the  inlet  to 
the  outlet  along  center  lines  was  36.6  feet. 

Concentrated  solutions  of  common  salt  and 
of  various  aniline  colors  were  added  to  the 
water  on  several  occasions  as  it  entered  the 
basin,  and  careful  observations  made  to  learn 
the  time  taken  for  passage  through  the  basin. 
It  was  found  that  the  first  water  so  charged 
passed  through  to  the  outlet  at  the  contract 
rate  of  flow  in  about  15  minutes.  The  water 
containing  the  greatest  amount  of  these  solu 
tions  passed  through  in  58  minutes,  but  the 
dilution  was  so  great  that  it  was  just  2  hours 
before  the  last  traces  of  the  substances  dis 
appeared  from  the  water  as  it  left  the  settling 
basin.  In  explanation  of  the  short  period 
which  elapsed  before  the  first  appearance  of 
the  substances  at  the  outlet  it  is  to  be  stated 
that  in  the  baffle-wall  opposite  the  mouth  of 
the  main  inlet  water-pipe  there  was  an  open 
ing,  i  to  2  square  inches  in  area,  through 
which  passed  an  iron  rod  0.5  inch  in  diameter. 

Drainage. — A  4-inch  flap  valve  located  in 
one  corner  of  the  settling  basin  was  used  as 
a  sludge  outlet.  No  provision  was  made  to 
drain  to  this  valve,  the  floor  of  the  chamber 
being  level. 

Cleaning. — No  special  arrangements  were 
made  for  cleaning. 

JEWELL  SETTLING  CHAMBER. 

The  settling  chamber  together  with  the 
filter  was  included  in  one  large  circular 
wooden  tank,  14.0  feet  high  and  13.5  feet  out 
side  diameter. 


The  sides  were  made  of  3  by  g-inch  cypress 
staves,  and  the  bottom  of  two  layers  of  3-inch 
pme  planks.  The  hoops  were  eleven  in  num 
ber;  the  first  and  sixth  were  4.5  byo.iSinches, 
the  second,  third,  fourth,  and  fifth  were  4  by 
o.  12  inches,  and  the  upper  five  were  3  by  0.12 
inches.  All  of  them  were  made  of  wrought 
iron. 

At  a  distance  of  6.79  feet  above  the  floor 
of  the  tank  was  a  second  floor  3  inches  thick, 
which  formed  the  lower  floor  of  the  filter 
tank.  It  was  supported  on  eight  8  by  8-inch 
white-pine  posts,  four  8  by  lo-inch  timbers 
forming  the  floor-beams. 

The  lower  part  of  the  tank  was  used  as  the 
settling  chamber;  the  floor  and  sides  of  the 
tank  forming  the  bottom  and  sides  of  the  set 
tling  chamber,  respectively,  while  the  bottom 
floor  of  the  filter  formed  the  top  of  the  set 
tling  chamber.  The  general  dimensions  as 
shown  on  the  plan  were:  diameter,  13.0  feet, 
and  height,  6.89  feet. 

Inlet  Water-f>ife. — This  pipe  was  of  wrought 
iron  and  was  5  inches  in  diameter.  It  was  con 
nected  to  the  side  of  the  chamber  by  a  flange 
joint.  The  river  water  contained  in  it  was 
under  from  45  to  65  pounds  pressure,  and  was 
taken  from  the  force  main  leading  to  the  dis 
tributing  reservoir. 

Inside  the  chamber  there  was  a  single- 
seated  valve  operated  by  a  float  in  the  filter 
above,  and  designed  to  control  the  flow  into 
the  settling  chamber. 

Chamber  Outlet. — The  outlet  from  the 
chamber  was  in  the  center,  through  an  8-inch 
central  well  passing  no  through  the  filter. 

Elevations. — The  elevations  in  feet,  with  the 
bottom  of  the  sand  laver  as  the  datum  plane, 
were  as  follows: 

Center  of  inlet  water-pipe.  .  .   -6.05 

Floor  of  chamber -  7.61 

Roof  of  chamber -  0.82 

Height. — The  total  height  of  the  chamber 
was  6.79  feet,  and  the  height  under  the  beams 
supporting  the  floor  of  the  filter  was  5.96  feet. 

Area. — The  gross  area  of  the  settling  cham 
ber  was  132.7  square  feet.  The  area  deduct 
ing  the  supports  for  the  filter  floor  was  129.2 
square  feet. 

Capacity.- — The  total  capacity  of  the  cham 
ber  was  about  879  cubic  feet. 


WATER   PURIFICATION  AT  LOUISVILLE. 


Storage  Period. — Assuming  complete  dis 
placement  of  the  water,  the  length  of  time  re 
quired  for  the  water  to  pass  from  the  inlet 
to  the  outlet  pipe  at  the  contract  rate  (250,- 
ooo  gallons  per  24  hours)  was  36  minutes. 

The  flow  of  water  through  the  chamber  was 
traced  by  the  application  of  salt  and  various 
aniline  colors  in  experiments  similar  to  those 
described  in  the  case  of  the  Warren  System. 
Under  the  above-stated  contract  rate  of  flow 
the  water  charged  with  these  substances  ap 
peared  at  the  outlet  in  about  8  minutes  after 
their  application  at  the  inlet;  the  period  of 
passage  of  the  water  containing  the  greatest 
amount  of  these  substances  when  it  reached 
the  outlet  was  22  minutes;  and  the  last  ap 
preciable  trace  of  these  substances  in  the 
water  as  it  left  the  outlet  disappeared  in  48 
minutes  after  application  at  the  inlet. 

Inspection. — A  manhole  was  provided  at 
a  convenient  location  to  allow  of  inspection 
of  the  settling  chamber. 

Drainage. — An  8-inch  valve  was  connected 
to  the  side  of  the  chamber  at  the  bottom  by 
means  of  a  flange  joint.  This  valve  discharged 
into  a  barrel  connected  with  the  sewer.  The 
settling  chamber  could  be  drained  completely 
through  this  valve  provided  its  contents  were 
quite  liquid.  The  floor  of  the  chamber  was 
level,  however,  so  that  mud  and  slime  had  to 
be  swept  or  shoveled  out. 

Cleaning. — It  was  intended  to  flush  out  the 
settling  chamber  by  allowing  waste  wash- 
water  to  flow  over  into  the  central  well  from 
the  filter  above,  and  discharge  into  the  set 
tling  chamber.  A  curved  half-pipe  4  inches 
in  diameter,  which  was  fastened  to  and  turned 
with  the  agitator  shaft,  was  used  as  a  trough 
to  direct  the  flow  to  different  parts  of  the 
chamber.  This  did  not  prove  effective,  how 
ever,  and  the  method  of  cleaning  resorted  to 
was  by  hand,  aided  by  occasional  flushings 
from  the  inlet  water-pipe. 

WESTERN  SETTLING  CHAMBER. 

The  Western  Pressure  Filter  and  the  set 
tling  chamber  used  by  both  filters  were  con 
tained  in  a  large  steel  cylinder  made  of  0.62- 
inch  plates.  It  was  22.5  feet  long  and  8.0  feet 
in  inside  diameter.  The  ends  were  dome- 
shaped,  curving  outwards  1.25  feet.  This 


cylinder  was  divided  in  the  center  by  two 
curved  partitions.  The  partition  plates 
touched  at  the  center  and  were  bolted  to 
gether.  The  vertical  joints  were  all  lapped, 
and  the  horizontal  ones  were  all  butt-joints 
with  two  cover  plates.  Two  lines  of  staggered 
rivets  0.75  inch  in  diameter  were  used 
throughout.  The  total  weight  of  the  empty 
cylinder  was  said  to  be  27,000  pounds. 

The  west  half  of  the  cylinder  was  used  for 
the  settling  chamber,  the  east  half  for  the 
pressure  filter.  This  chamber  was  11.15  ^eet 
long  in  the  center,  8.71  feet  long  on  the  sides, 
and  8.0  feet  in  inside  diameter. 

Supply  of  River  Water. — The  supply  for  the 
Western  Systems  was  at  first  furnished  by  the 
same  pipe  which  supplied  the  Warren  and 
Jewell  systems  with  river  water  under  from 
45  to  65  pounds  pressure  from  the  force  main 
to  the  Crescent  Hill  Reservoir.  The  varia 
tions  in  pressure  were  due  to  the  variations  in 
draft  on  the  supply-pipe. 

Objections  were  made  to  this  by  the  West 
ern  Filter  Company  on  account  of  the  varia 
tions  in  pressure  caused  by  the  operation  of 
the  other  systems.  Therefore,  on  Feb.  29, 
1896,  a  new  4-inch  river-water  pipe  was  laid 
from  the  force  main,  to  be  used  solely  by  the 
Western  Systems.  After  the  change  the 
pressure  was  held  very  closely  between  60  and 
65  pounds. 

Up  to  April  7  this  pipe  was  connected  di 
rectly  with  the  settling  chamber.  Among 
the  changes  made  during  the  period  from 
April  7  to  May  8  was  the  introduction  of  a 
Worthington  pump  on  this  pipe.  This  was 
done  with  the  view  to  obtaining  better  equali 
zation  of  the  pressure  in  the  water-pipe,  and 
also  to  operate  a  pair  of  auxiliary  plunger 
pumps  which  were  used  for  applying  the 
chemical  solution  as  already  described  in 
Chapter  II. 

Pumping  Engine. — The  pumping  engine 
was  of  the  the  H.  R.  Worthington  pattern. 
The  main  dimensions  were  g-inch  steam- 
cylinder,  8.5-inch  water  cylinder  and  lo-inch 
stroke.  It  was  a  single-expansion  duplex  en 
gine.  The  steam  was  supplied  by  a  i. 5-inch 
covered  pipe.  The  exhaust  was  a  2-inch  pipe, 
open  to  the  atmosphere. 

Inlet  Water-pipe. — As  first  used  the  inlet  to 
the  settling  chamber  was  a  simple  pipe  with  a 


COAGULATION  AND   SEDIMENTATION  BY  ALUMINUM   HYDRATE.         61 


flange  joint  screwed  on  to  the  bottom  of  the 
cylinder.  With  the  other  changes  in  April 
this  was  modified,  and  a  distributing  pipe  was 
inserted  in  the  chamber.  This  distributer  was 
formed  by  a  6-inch  nipple  12  inches  long 
screwed  into  the  upper  side  of  the  Mange  joint 
above  mentioned;  a  6-inch  tee  with  its  long 
arm  horizontal,  and  two  lengths  of  6-inch 
pipe  each  2.5  feet  long  capped  at  the  outer 
end.  On  each  side  of  the  nipple  and  pipes 
was  a  line  of  holes  1.5  inches  in  diameter. 
There  were  two  holes  in  the  tee,  four  in  each 
nipple  and  one  in  the  center  of  each  cap.  The 
center  of  the  holes  was  1.30  feet  above  the 
floor  of  the  chamber. 

Outlet. — The  outlet  from  the  settling-cham 
ber  was  a  simple  6-inch  pipe  connected  to 
the  top  of  the  cylinder  by  a  flange  joint. 

This  pipe  led  down  to  the  front  of  the  cyl 
inder  and  joined  a  tee,  to  the  ends  of  which 
were  attached  the  pipes  leading  to  the  press 
ure  and  gravity  filters,  respectively. 

Elevations. — The  principal  elevations  in 
feet,  with  the  bottom  of  the  sand  layer  of  the 
pressure  filter  as  the  datum  plane,  were  as 
follows: 

Center  of  inlet  pipe -0.80 

Bottom  of  cylinder  (inside) .  .    -2.15 
Top  of  cylinder  (inside) +  5.85 

Capacity.- — The  capacity  of  the  chamber 
was  503  cubic  feet. 

Storage  Period. — Assuming  complete  dis 
placement  in  the  chamber  the  storage  interval 
at  the  contract  rate  (250,000  gallons  per  24 
hours)  was  22  minutes. 

Experiments  with  salt  and  various  aniline 
colors,  similar  to  those  described  in  connec 
tion  with  the  other  systems,  were  made  to 
trace  the  flow  of  water  through  the  settling 
chamber.  At  the  contract  rate  of  flow,  as 
stated  above,  the  water  containing  these  ap 
plied  substances  first  appeared  at  the  outlet  in 
about  2  minutes  after  their  application;  the 
water  containing  the  largest  proportion  of 
these  substances  passed  through  the  chamber 
in  9  minutes;  and  the  last  appreciable  traces 
of  the  salt  and  dyes  disappeared  from  the 
water  at  the  outlet  in  27  minutes  after  their 
application  to  the  water  at  the  inlet. 

With  both  filters  in  operation  at  the  con 


tract  rate,  the  storage  period  in  this  chamber 
would  be  only  one-half  as  long  as  stated 
above. 

Inspection. — The  settling  chamber  could  be 
inspected  by  removing  a  manhole  placed 
about  in  the  center  of  the  upper  front  quad 
rant.  A  hand-hole  was  also  provided,  occupy 
ing  a  similar  position  in  the  lower  quadrant. 

Drainage. — The  construction  was  such  that 
there  was  no  convenient  method  of  draining 
the  chamber.  The  inlet  pipe  at  its  lowest 
point  was,  however,  provided  with  a  tee,  one 
arm  of  which  was  plugged.  By  removing  this 
plug  the  water  could  be  drained  out  to  the 
level  of  the  distributing  pipe.  As  no  arrange 
ments  were  made  to  carry  off  the  water  from 
this  plug  it  was  used  but  little.  The  usual 
method  was  by  siphonage  through  the  man 
hole  in  the  upper  part  of  the  chamber. 

Cleaning. — Handwork  was  mainly  relied 
upon  for  cleaning.  By  a  system  of  valves  and 
piping,  connection  was  formed  between  the 
wash-water  and  chamber  outlet  pipes  so  that 
wash-water  could  be  turned  in  from  above  to 
aid  in  flushing  the  chamber. 

PURIFICATION  OF  THE  OHIO  RIVER  WATER 

BY  SEDIMENTATION  IN  THE 

SEVERAL  SYSTEMS. 

As  sedimentation  is  an  intermediate  step  in 
the  complete  purification  by  this  system  of  the 
Ohio  River  water,  and  as  it  varies  widely  ac 
cording  to  the  existing  conditions,  this  phase 
of  the  tests  was  not  made  the  subject  of  de 
tailed  daily  study.  Attention  was  given  to  the 
matter  in  a  general  way,  however,  with  the 
view  to  learning  its  practical  significance. 

Inspection  showed  very  quickly  that  the  de 
gree  of  purification  of  the  Ohio  River  water 
by  sedimentation  was  a  variable  factor  so  far 
as  the  removal  of  mud  was  concerned.  With 
the  same  river  water  sedimentation  increased 
with  the  amount  of  aluminum  hydrate 
formed  from  the  decomposed  alum  or  sul 
phate  of  alumina. 

This  would  be  naturally  expected,  of 
course,  because  the  greater  the  number  of 
minute  gelatinous  particles,  forming  centers 
of  coagulation,  the  greater  would  be  the  size 
and  weight  of  the  coagulated  masses  or 
flakes;  and,  in  turn,  the  greater  and  heavier 


62 


WATER   PURIFICATION  AT  LOUISVILLE. 


these  flakes  the  more  quickly  would  they  sub 
side  by  gravity  to  the  bottom  of  the  settling 
chambers. 

At  times  the  Ohio  River  water  had  sus 
pended  in  it  large  quantities  of  very  fine  silt 
and  clay,  of  which  the  individual  particles 
sometimes  ranged  as  small  as  o.ooooi  inch  in 
diameter.  It  was  after  heavy  rains  following 
a  long  period  of  drought  that  water  of  such 
a  character  was  found.  With  the  same 
amounts  of  aluminum  hydrate  in  two  samples 
of  river  water,  one  of  the  character  just  de 
scribed,  and  the  other  a  more  nearly  normal 
water  containing  the  same  amount  by  weight 
of  larger  suspended  matter,  the  latter  water 
is  far  more  purified  by  coagulation  and  sedi 
mentation  in  the  same  period  of  time  than  is 
the  former  water.  With  plain  sedimentation, 
without  coagulation,  similar  results  would  be 
obtained;  and  the  explanation  of  the  results 
just  described  is  that  the  coagulation  was 
quite  incomplete.  With  a  water  containing 
an  innumerable  quantity  of  very  finely  divided 
particles,  the  period  necessary  for  coagulation 
is  unusually  long;  and  it  appears  that,  in  some 
cases  at  least,  the  bulk  of  the  aluminum  hy 
drate  together  with  the  larger  suspended  par 
ticles  subside  before  a  large  portion  of  the 
fine  particles  is  coagulated. 

Another  factor  which  produces  a  marked 
effect  upon  the  degree  of  sedimentation  is  the 
period  of  time  during  which  the  coagulation 
and  subsidence  take  place.  The  actual  stor 
age  periods  under  normal  conditions  for  the 
respective  systems  have  already  been  pre 
sented  in  an  earlier  portion  of  this  chapter. 
These  storage  periods  were  complicated  in  a 
good  many  cases  by  washing,  repairing,  and 
modifying  the  filters  and  by  delays  occasioned 
by  the  filters  being  out  of  service  during  the 
night  (except  March  24-30  and  April  27  to 
June  6)  and  on  Sundays. 

During  the  six  weeks'  continuous  run  (Sun 
days  excepted),  from  April  27  to  June  6, 
twenty-nine  sets  of  bacterial  analyses  were 
made  of  the  river  water  before  treatment,  and 
of  the  corresponding  water  after  it  has  passed 
through,  under  normal  conditions,  the  War 
ren  settling  basin  and  the  Jewell  settling 
chamber,  respectively.  At  the  outset  the  fa 
cilities  for  taking  samples  of  the  water  after 
passage  through  the  Western  settling  cham 


ber  were  not  wholly  satisfactory.  During  the 
latter  part  of  the  period  (May  28  to  June  i) 
eight  samples  were  taken  from  this  system. 
The  average  results  of  these  analyses  are  com 
pared  with  the  corresponding  ones  from  the 
other  two  systems  just  after  the  next  table. 
In  the  next  table  are  recorded  the  results  of 
the  individual  analyses  with  the  percentages 
of  removal,  in  the  full  set  of  tests  of  the  War 
ren  and  Jewell  systems  upon  this  point.  The 
average  quantities  of  sulphate  of  alumina  ap 
plied  by  each  system  on  the  different  days 
are  given  in  Chapter  II. 

It  will  be  noted  that  these  results,  which  are 
tabulated  below,  are  quite  variable  with  re 
gard  to  the  percentages  of  removal.  This  was 
due  in  part  to  the  amount  of  applied  sulphate 
of  alumina  in  relation  to  the  quality  of  the 
river  water;  and  also  to  the  fact  that  there 
were  in  the  water  small  flakes  of  coagulated 

NUMBERS  OF  BACTERI A  PER  CUBIC  CENTI 
METRE  IN  THE  OHIO  RIVER  WATER 
BEFORE  AND  AFTER  PASSAGE  THROUGH 
THE  WARREN  SETTLING  BASIN  AND  THE 
JEWELL  SETTLING  CHAMBER.  RESPECT 
IVELY,  WITH  THE  PERCENTAGES  OF 
REMOVAL. 


Dale. 

_ 

in  Water  fi 

m 

1896. 

Warren 

Jrwdl 

River. 

Settling 

Settling 

Warren. 

Jewell. 

Basin. 

Chamber. 

April  28 

5  70" 

5  Soo 

4  3<» 

o 

25 

29 

7  loo 

2  800 

2  8OO 

60 

60 

3° 

3  700 

2  300 

1  700 

38 

54 

May    2 

5  600 

I   TOO 

4  too 

80 

27 

2 

9  OOO 

2  8OO 

7400 

69 

18 

4 

7  5oo 

2  9OO 

4  700 

6  1 

37 

<; 

9  ooo 

6  OOO 

4900 

33 

46 

6 

4  900 

I   800 

4400 

63 

10 

7 

5  ooo 

4  2(X> 

I  700 

16 

66 

1  1 

6  900 

2  40O 

3  500 

65 

49 

12 

7  100 

I  7<w> 

4  coo 

76 

44 

13 

4  200        i  ooo 

3  400 

7f> 

19 

M 

?  Son         I  500       ;        3  too 

74 

47 

15 

7  ?oo 

I  300             I  500             83 

So 

if) 

10900 

I  800 

2  400             83 

78 

18 

9  5°o 

I  Soo 

4  600             8  1 

52 

19 

7  800 

5  40" 

3  400 

26 

53 

20 

4  700        4  400 

2  3OO 

06 

;i 

21 

5  900        2  700 

4300 

54 

27 

22 

4  600        i  800 

2  400 

61 

48 

28 

14  900.       6  800 

II  900 

54 

20 

29 

33900 

6800 

21  2OO 

80 

37 

29  23  600 

I  400 

1  5  900 

94 

33 

30  28  7ooj       5  too 

20  300 

82 

29 

30  21  8ooi        5  100 

15  200 

77 

30 

Ji  ne    3   18  900,       2  200 

4  100 

88 

78 

'59  900!       2  800 

4  100 

72 

59 

'       5     6  200       2  400 

3  500 

61 

44 

5     5  ooo        i  600 

3  100 

68 

38 

Averages   10500        3100 

5  9°o 

61 

43 

COAGULATION  AND   SEDIMENTATION  BY  ALUMINUM   HYDRATE. 


material,  containing  bacteria  enveloped  within 
and  around  them,  and  which  were  of  necessity 
broken  up  in  an  incomplete  and  irregular 
manner  as  they  were  mixed  with  the  culture 
medium  for  bacterial  analysis.  That  is  to  say, 
it  was  practically  impossible  to  get  all  the 
bacteria  in  these  Makes  separated  into  single 
cells  so  that  each  colony  on  the  culture 
medium  should  represent  only  one  bacterium, 
as  the  method  of  analysis  called  for. 

During  the  period  from  May  28  to  June  I, 
inclusive,  when  the  river  water  contained  the 
greatest  amount  of  very  finely  divided  par 
ticles,  and  when  it  was  most  difficult  to  coagu 
late,  the  average  results  of  bacterial  purifica 
tion  by  coagulation  and  sedimentation  in  the 
three  systems  were  as  follows: 


System. 

Number  of  Bacteria  per 
Cubic  Centimeter. 

Percentage  Remoral. 

Warren 

5  ooo 

So 

Jewell 

1  6  900 

31 

Western 

16  600 

32 

(River) 

24600 

On  June  5  and  6  four  samples  of  river 
water  before  and  after  passage  through  the 
Warren  settling  basin  and  the  Jewell  settling 
chamber,  respectively,  were  collected  under 
normal  conditions  and  mixed  together  for 
chemical  analysis.  The  results  of  the  analyses 
showed  that  59  and  18  per  cent.,  respectively, 
of  the  suspended  matter  in  the  river  water 
were  removed  in  these  two  systems  by  coagu 
lation  and  sedimentation. 

These  results  show  very  forcibly  the  great 
economical  importance  of  long  storage  peri 
ods  in  order  to  allow  the  coagulated  material 
to  subside,  especially  as  the  removal  in  the 
Warren  System  of  more  than  three  times  that 
in  the  Jewell  System  was  effected  with  only 
65  per  cent,  of  the  sulphate  of  alumina  em 
ployed  in  the  latter  system. 

The  examinations  of  the  removal  of  sus 
pended  matter  of  the  river  water  in  the  West 
ern  settling  chamber  indicated  that  it  was 
more  variable  than  in  the  case  of  the  other 
systems,  but  on  an  average  about  equal  to 
that  by  the  Jewell  settling  chamber. 

During  June  and  July  several  sets  of  analy 
ses,  both  chemical  and  bacterial,  were  made 
of  the  river  water  before  and  after  it  had  re 
mained  over  night  or  over  Sundav  in  the  sev 


eral  respective  settling  chambers.  The  re 
sults  of  the  analyses  bore  out  the,  observations 
as  to  the  appearance  of  the  water  in  the  set 
tling  chambers,  showing  in  practically  every 
case  a  removal  of  more  than  90  per  cent,  of 
both  bacteria  and  suspended  mineral  and 
organic  matter,  while  in  several  instances  the 
removal  was  more  than  99  per  cent. 

These  last  data  show  very  conclusively  the 
great  economical  importance  of  coagulation 
and  sedimentation  in  the  purification  of  such 
muddy  water  as  that  of  the  Ohio  River. 

They  also  show  the  superiority  in  this  re 
spect  of  the  Warren  over  the  other  systems, 
owing  to  a  longer  storage  period  in  the  set 
tling  chamber,  during  which  sedimentation 
takes  place.  Furthermore,  this  evidence  is 
abundant  proof  that  in  all  these  systems  the 
storage  period  in  the  settling  basin  and  cham 
bers  is  too  short  by  far  to  allow  full  benefit 
and  economy  to  be  derived  from  sedimenta 
tion. 

Owing  to  the  great  practical  importance  of 
sedimentation,  some  special  experiments  were 
made  for  the  purpose  of  obtaining  more  in 
formation  on  this  subject,  as  will  be  found  in 
the  next  section  of  this  chapter.  During  1897 
additional  experiments  were  made,  and  the  re 
sults  are  recorded  in  Chapter  XV. 

SPECIAL  INVESTIGATIONS  UPON  THE  DEGREE 
OF  PURIFICATION  OF  THE  OHIO  RIVER 
WATER  BY  SEDIMENTATION  UNDER 
VARYING  CONDITIONS,  BOTH  WITH  AND 
WITHOUT  COAGULATION  BY  ALUMINUM 
HYDRATE,  AND  WITH  SPECIAL  REFER 
ENCE  TO  THE  INFLUENCE  OF  THE  PERIOD 
OF  SUBSIDENCE. 

This  set  of  experiments  was  made  with  the 
aid  of  a  settling  pipe,  20  inches  in  diameter 
and  24  feet  deep,  placed  in  the  boiler  house. 
Suitable  piping  arrangements  were  made  to 
allow  flushing,  filling,  and  draining  the  pipe, 
and  at  the  sides  of  the  pipe  was  placed  a  series 
of  pet  cocks  through  which  samples  of  water 
could  be  drawn  at  stated  distances  from  the 
bottom. 

The  results  of  these  experiments  are  given 
in  the  following  table.  Except  in  those  cases 
where  the  regular  samples  (numbers  in  paren 
theses)  for  daily  analyses  of  the  river  water 


64 


WATER  PURIFICATION  AT  LOUISVILLE. 


were  used,  special  serial  numbers  were  given 
to  samples  collected  for  this  purpose. 

The  distances  from  the  bottom  of  the  pipe 
to  the  tap  from  which  the  sample  was  taken 
are  given  under  the  heading,  source  of  sample. 
Analyses  were  made  for  the  determination  of 
the  total  suspended  solids  (insoluble  residue 
on  evaporation),  and  also  of  the  number  of 
bacteria  in  the  water.  As  explained  above, 
the  latter  determination  was  complicated  by 
the  presence  of  masses  of  suspended  matter 
in  the  water  which  made  it  difficult  to  sepa 
rate  the  individual  bacteria.  Another  factor 
affecting  the  determination  of  the  percentage 


removal  of  the  bacteria  was  the  high  and  un 
equal  temperature  of  the  water  in  the  pipe  at 
different  heights  and  at  different  times  during 
the  same  experiment.  The  temperature 
probably  exerted  a  retarding  influence  upon 
subsidence,  but,  on  the  other  hand,  the  gen 
eral  conditions  of  sedimentation  in  a  small  tank 
are  more  favorable  than  in  a  large  basin  or 
reservoir.  In  those  cases  where  no  coagulants 
were  applied  it  is  probable  that,  under  the 
conditions  of  practice  with  longer  periods  of 
subsidence,  the  variation  in  the  amount  of 
suspended  matter  in  the  water  at  different 
depths  would  be  reduced  materially. 


COAGULATION  AND   SEDIMENTATION   BY  ALUMINUM  HYDRATE.         65 
RESULTS   OF   SEDIMENTATION   EXPERIMENTS. 


Experiment. 

Applied 
Sulphate  of 

Grains  per 
Gallon. 

Sample. 

Period  of 
Subsidence. 
Hours. 

Tempera- 
Deg'rees  C. 

Suspended  Solids. 

Bacteria. 

Number. 

Date. 

1896. 

Number. 

Source. 

Parts  per 
Million. 

Per  Cent 
Removed. 

Per  Cubic        Per  Cent 
Centimeter.      Removed. 

I 

2 
3 

4 
5 
6 

7 
8 

9 

10 

ii 

May    29 

June     I 
June    2 

June    4 
June    6 
June  10 

June  10 
June  ii 

June  II 

June  12 
June  12 

O.O 

0.0 
0.0 

O.O 
0.0 

4.0 

o.o 
3-0 

2.0 
2.0 

3.0 

I 
2 
3 
4 

5 
6 
7 
8 

9 

10 

1  1 
13 
14 
'5 
16 
18 
19 

20 
22 
23 
24 
25 
27 
28 
29 
31 
32 

33 
34 
36 
37 
38 
40 
41 
(626) 
50 
5i 
52 
53 
54 
57 
58 
59 
60 
61 
62 
63 
64 
66 
67 
69 
70 
71 
72 
73 
74 
75 
77 
78 
79 
80 
(632) 
81 
83 
84 
86 
87 
88 

River. 
2         feet 
4 
11.75     " 

20 
2              " 
4 
11.75      " 
20 
River 
2         feet 
11.75     " 
20 
River 
2          feet 
11.75     " 

20 
2              " 
11.75      " 
20 

River 
2         feet 
11.75     " 
20 
2             " 
11.75      " 
20             " 
River 
2         feet 
11.75     " 
20 

2              " 
11.75       " 
20 
River 
2         feet 
6 
11.75     " 

20 
2              " 
2O              " 

"•75     " 
River 
2         feet 
11.75     " 
20             " 

River 
2        feet 
20          " 

2              " 
2O              " 

"-75     " 
River 
2         feet 
11.75     " 
20 
2             " 
20             " 

ir.75    " 
11.75     " 
11.75    " 
River 
2         feet 
20          " 
2             " 
20             " 
River 
2         feet 

O 
24 
24 
24 
24 
48 
48 
48 
48 
O 
24 
24 
24 
O 
24 
24 
24 
48 
48 
48 
0 

24 

24 

24 

48 

48 
48 

O 
24 

24 

24 

48 

48 

48 

O 

I 
I 
I 
I 
3 

•J 

O 

18 
18 
18 

O 

I 
I 

3 
3 
4-5 
o 
i 
i 
i 
3 
3 
6 

12 

16 
o 
i 
i 
3 
3 

0 

i 

590 
32O 

45-8 

286 
262 
170 

51-5 
55-6 
71.2 

1  60 
90 
390 
254 
226 
'94 
936 
"24 

72.  S 
84.7 

34-9 
42.1 
50.2 

22.6           

580 
5'4 
504 
338 

22S 

38.0 
45.1 
46.1 
63-9 

75.6 

30.O 

33-5 
31.0 

29.2 
33-o 
35-8 
32.8 
34-8 
36.0 

220 

218 

150 

186 

122 
92 
22O 

31-3 
31-9 
53-1 
41.9 
61.9 
71.2 

I46 

130 

118 

114 

88 
80 
413 
17 
19 
20 

'9 
9 
10 
"5 
298 

33-6 
40.9 
46.4 

48.2 
60.0 
63.6 

29.8 
32.0 
33-7 

2  gOO 
2  700 
fOO 

52.4 
55-7 
91  .8 

95-9 
95-4 
95.1 
95-4 
97.8 
97-7 
95.1 

I  6OO 

I   OOO 

I  300 

400 

87.4 
92.  i 
89.8 
96.9 

900 

92.9 

256 
198 
152 
296 

14.1 

33-6 
45.6 

8  500 
700 
400 

19 
18 
ii 
ii 

9 

252 

93.6 
93-9 
96.3 

96.3 
97-0 

91.8 
95-3 

18 
14 
ii 

4 
3 
3 

2 
2 

92.8 
94-4 
95.6 
98.4 
98.8 
98.8 
99.2 
99.2 

4  ioo 
500 
300 

'9 

19 

6 
6 

245 

91.9 
91.9 
97-4 
97-4 

87.8 
92-7 

10 

95-9 

66 


WATER   PURIFICATION  AT  LOUISVILLE. 

RESULTS    OF    SEDIMENTATION    EXPERIMENTS.—  Continued. 


Experi 

ment. 

Applied 
Sulphate  of 

Sam 

pie. 

Period  of 

Tempera- 

Suspende 

d  Solids. 

Bact 

-ria. 

Date 

Grains  per 

Hours. 

Degrees  C. 

' 

1896. 

Gallon. 

Source. 

MtllioPn. 

Removed. 

Removed. 

s 

2          feet 

78  o 

06 

80.3 

8l    2 

OS 

88 

84  6 

2O           " 

89.6 

6 

89  6 

800 

I.O 

(642) 

River. 

46 

2         feet 

96  6 

6 

98  6 

June  16 

0.5 

(646) 

River. 

8  800 

2         feet 

63  6 

108 

76  8 

80  3 

64  7 

80  3 

15 

1  .0 

River. 

248 

8  300 

64 

3  800 

85  g 

86  7 

28 

88   7 

16 

June  17 

0.5 

116 

266 

266 

118 

20          " 

119 

2              " 

3 

98 

96 

121 

1  1  -75     " 

18 

81.6 

86.5 

17 

June  18 

1  .5 

(651) 

River. 

278 

91   8 

800 

89  6 

95.7 

98.9 

18 

June  18 

0.25 

126 

127 
128 

2          feet 
20           " 

I 
I 

299 

o 

12  2OO 

20  8 

Ig 

0.25 

(655) 

River. 

132 

2         feet 

I 

84 

80.0 

3  800 

84 

80  o 

63  8 

134 

2              " 

3 

20 

June  ig 

0.75 

136 

River. 

2         feet 

138 

20          " 

I 

20          " 

3 

182 

28  6 

141 

11.75     " 

20 

80 

81.3 

21 

June  20 

2.O 

(658) 

River 

142 

2         feet 

i 

37 

87.5 

89.8 

I 

91  8 

2              " 

3 

18 

92.8 

145 

22 

I  .O 

146 

River. 

25  8 

M7 

148 

2         feet 

20 
2              " 

I 

i 

28.O 

35-5 

46 

48 

82.9 

82.2 

3  500 

2  500 

63.9 
74.2 

98  8 

23 

June  20 

O.O 

151 

261 

152 

2         feet 

22 

23.  7 

153 

H-75     " 

COAGULATION  AND   SEDIMENTATION^  BY  ALUMINUM  HYDRATE. 
RESULTS   OF   SEDIMENTATION    EXPERIMENTS.— Continued. 


67 


Experiment. 

Applied 
Sulphate  of 

Grains  per 
Gallon. 

Sample. 

Period  of 

Subsidence. 
Hours. 

Tempera- 
Degrees  C. 

Suspended  Solids. 

Bacteria. 

Number. 

Date. 

,896. 

Number. 

Source. 

Parts  per 
Million. 

Per  Cent 
Removed. 

Per  Cubic 

Per  Cent 
Removed. 

23 
24 

25 
26 
27 

28 
29 
30 

31 

32 

33 

34 

35 

June  20 
June  23 

June  23 
June  24 
June  24 

June  25 
June  26 
June  27 

June  29 

July     I 
July    2 

July      6 
July    6 

o.o 

3.0 

1  .0 

2.O 
0-75 

0.75 
0-75 
0.75 

O.O 

0.0 
1.0 

2.0 

0.75 

154 
'55 
156 
157 
(660) 
158 
159 
1  60 
161 
162 
163 
164 
165 
1  66 
(668) 
167 
1  68 
169 
170 
171 
172 
173 
174 
175 
176 
(678) 
177 
178 

179 

1  80 
181 
(681) 
182 
183 
184 
185 
1  86 
(684) 
187 
188 
189 
i  go 
191 
192 
(686) 
193 
194 
195 
196 
(692) 
202 
203 
204 
205 
206 
207 
208 
209 
(704) 

210 
211 
212 
213 
2I4 
215 

216 

217 

218 

20         feet 

2              " 

11.75     " 
20           " 
River 
2         feet 

20              " 

2           " 
20             " 
River 

2         feet 
20             " 
2               " 

20          " 
River 

2         feet 
20           " 

2              " 

20           " 
River 
2         feet 
20           " 

2              " 

20          " 
11.75     " 
River 
2         feet 
20          " 
2             " 
20 
11.75     " 
River 
2         feet 
20          " 

2               " 

20          " 
11.75     " 
River 
2         feet 
20           " 
2           " 
20             " 

11.75   " 
11.75    " 

River 
2         feet 
20          " 
2           " 
20          " 
River 
2         feel 

20              " 

River 
2         feel 
20          " 

2             " 
2O             " 
11-75      " 

River 
2         feet 
20             " 
2              " 

20           " 
River 
2         feel 
20             " 
2             " 
20             " 

22 
48 
48 
48 
0 

I 

I 
3 
3 
o 
i 
i 
3 
3 

0 

i 

i 
3 
3 

0 

i 

i 
3 
3 
20 
O 
I 
I 

3 
3 
24 
o 
i 
i 
3 
3 
24 

0 

i 
i 

3 
3 
30 
48 

0 

3 
3 
24 
24 
o 
24 
24 
o 
I 
I 
3 
3 
17 
o 
i 
i 
3 
3 
o 
i 
i 
3 
3 

37-2 

129 

125 
67 
48 
235 
31 
25 
9 
5 
218 
42 
39 
32 
32 
446 
54 
41 
22 
22 
267 

52.6 
52.1 
74-3 
81.6 

3900 
900 
900 

65.2 
92.0 
92.0 

26.2 
26.2 
30.0 

86.8 
89-3 
96.2 

97-8 

400 
500 

95-7 
94-7 

27.0 
27.0 
32.0 

8OOO 
4600 

39°° 
2  2OO 

80.7 
82  i 
85.3 
85.3 

42.5 

51-3 
72.5 

27.4 
27.0 
36.5 

87.7 
90.6 
94.8 

94.8 

3  too 
8  ooo 
4400 
4  200 
13  Soo 

39-2 

13-7 
17.6 

I48 
M7 
58 
58 
T9 
321 

59.6 
59-8 
84.1 
84.1 
94.8 

8  loo 

II  200 

7  800 

IO  *00 

2800 

5  300 

41.4 
18.8 
43-5 
26.0 
69.7 

27-3 

62.2 

109              66.1 

46              85.5 
35              89-i 
28              91.2 

2  400 

2  COO 

3  Sou 
500 
6  ooo 

2  400 

2  300 

700 
I  400 
400 

7900 

6  loo 

7  700 
4300 

54-7 
56.6 
28.2 
90.6 

193 
114 

52 

48 
24 
358 
358 
232 

100 

88 

34-8 
58.2 
82  4 
83-7 
92.0 

0. 

35-2 
72.1 

75-3 

60.0 
61.6 
88.3 
76.6 
93-3 

26.5 
27.0 
36.0 

22.8 
2.6 

45-6 

18 
5°5 
493 
465 
276 
193 
856 
435 
336 
636 
1552 
1385 
i  248 
796 
43° 
244 
40 
30 

12 

8 
395 
209 
199 
"5 
103 

95-1 

400 

94-9 

25-5 
26.0 

34-8 

2.4 
7-9 
45-3 
61.8 

10  900 
9  200 
3  ooo 
4  200 

12.8 
26.  5 
76.0 
66.4 

26.5 
29-3 
38.2 
23-5 
25.8 
31-3 

49-2 
60.7 

8  400 
4  200 

5-2 
15-3 
23.7 
51-3 
73-8 

26.3 
26.0 
34-5 

6300 

2  2OO 
I  3OO 
I  IOO 
600 
Q500 

7  100 
7400 
3600 
4  loo 

83.6 
87.7 
95.1 
96.7 

65.0 
79-4 
82.5 
90.5 

47.1 
49-5 
70.9 
73-9 

25-2 
22.0 
62.1 
56.8 

68 


WATER  PURIFICATION  AT  LOUISVILLE. 

RESULTS    OF    SEDIMENTATION    EXPERIMENTS.— Concluded. 


Exper 

men, 

Applied 
Sulphate  of 

San 

pie. 

Period  of 

Tempera- 

Suspend 

d  Solids. 

Bact 

Number. 

Date. 

1896. 

Grains  per 

Number. 

Source. 

Hours. 

Degrees  C. 

Parts  per 
Million. 

Pei  Cent 

Per  Cubic 

Per  Cent 
Removed. 

Si   8 

16 

Inlv       i 

(707) 

222 

2         feet 

3 

26.5 

438 
188 

16.5 
26   i 

3700 

31-5 

224 
225 
226 

"•75    " 
"•75    " 
n.  75    " 
River 

24 
48 
72 

34-0 
34-3 

35-7 

22g 
'77 

153 
087 

56-3 
66.2 
70.8 

3500 

1   IOO 
2  400 

35-2 
7Q.6 

55-5 

^S 

227 

(T2t) 

II  .75  feet 
River 

24 

34-6 

21 

45-7 

I  300 

6  Soo 

84.  1 

23O 
231 

2        feet 
20            " 

3 
28 

27-3 
37-5 

1  66 
154 

20.2 
26.0 
64    4 

7  500 
5  500 

8.5 
32.8 

a6 

34  6 

6  1 

•ic   8 

79  8 

600 

(73O) 

July    18 

235 

(744) 

11.75  feet 

24 

35-  S 

28 
637 

93-o 

I  COO 

gi  .6 

248 
249 
250 
(767) 

11.75  feet 
"•75    " 
11.75    " 
River 

72 

120 
144 

33-4 
35-5 
36.7 

202 
142 
131 

68.2 
77-7 
79-4 

2  IOO 

600 
7OO 

72.4 
92.1 
90.8 

251 
252 

11.75  feet 
"•75    " 

24 

144 

32-9 
3S-9 

872 
195 

74-0 
94-2 

5  100 

10 

85-0 
99-9 

COAGULATION  AND   SEDIMENTATION  BY  ALUMINUM  HYDRATE.         69 


NUMBER  OF  BACTERIA  PER  CUBIC  CENTI 
METER  IN  THE  OHIO  RIVER  WATER 
AFTER  PASSAGE  THROUGH  THE  DIS 
TRIBUTING  RESERVOIR  AND  A  PORTION 
OF  THE  DISTRIBUTING  PIPE  OF  THE 
LOUISVILLE  WATER  COMPANY. 

In  the  next  table  are  recorded  the  results 
of  bacterial  analyses  of  tap  water  collected 
in  the  city  of  Louisville.  In  all  cases  the 
water  was  allowed  to  run  from  the  faucet  for 
some  minutes  before  the  sample  was  col 
lected.  The  place  of  collection  was  419  West 
Chestnut  Street  up  to  Feb.  i,  1896,  and  at 


820  South  Second  Street  for  the  remainder  of 
the  time. 

On  its  way  to  the  city  the  river  water  is 
pumped  to  the  Crescent  Hill  Reservoir,  which 
has  a  capacity  of  100  million  gallons,  equiva 
lent  to  about  six  times  the  average  daily  con 
sumption  of  the  city. 

The  chief  value  of  these  results  is  that  they 
show  a  removal  by  subsidence  and  passage 
through  the  distributing  pipes  of  about  80  per 
cent,  of  the  bacteria  originally  present  in  the 
water  as  it  was  pumped  from  the  river.  In 
this  connection  reference  may  be  made  to  the 
results  of  bacterial  analyses  of  the  river  water 
already  presented  in  Chapter  I. 


NUMBER   OF    BACTERIA    PER   CUBIC   CENTIMETER    IN   THE    TAP-WATER    OK   THE   CITY   OF 
LOUISVILLE,   BY    DAYS,   IN    1895-96. 


' 

pn  . 

ay. 

128 

I  OOO 

i  600 

116 

I  2OO 

I  IOO 

800 

I  QOO 

8OO 

1  08 

i  848 

' 

6 

119 

2  5OO 

2900 

6  700 

2  OOO 

6  900 

I  5OO 

goo 

I  800 

8 

178 

I  SOO 

I  ";oo 

228 

i  700 

2  000 

i  200 

1  18 

-no 

118 

4 

3 

13 

104 

I  OOO 

IOO 

400 

3  5oo 

6  200 

2  OOO 

I  3OO 

2  200 

2  3OO 

136 

i  800 

2  2OO 

I  2(X) 

2  20O 

2  IOO 

1  6 

i6j 

I  OOO 

800 

3  800 

6OO 

2  6OO 

I  OOO 

18 

368 

800 

QOO 

I  6OO 

700 

I  Soo 

20 

321 
nf> 

I  300 

I  400 

4  800 

3300 

800 

4  ooo 

9700 

2  7OO 

2  IOO 
I  IOO 

588 

I  OOO 

* 

ooo 

288 

I  IOO 

400 

r  700 

2  OOO 

26 

27 

28 

456 

700 

I  OOO 

i  300 

7  ioo 

I  300 

1  800 

2  OOO 

3500 

29 

4i8 

800 

10900 

8  200 

600 

2  OOO 

6o<> 
1  600 

i  QOO 

900 

3900 

2  2OO 

I  2OO 

WATER   PURIFICATION  AT  LOUISVILLE. 


CHAPTER   V. 

DESCRIPTION  OF  THE  FILTERS  THROUGH   WHICH  THE  RIVER  WATER  PASSED  AFTER 
COAGULATION  BY  ALUMINUM   HYDRATE  AND  PARTIAL  PURI 
FICATION  BY  SEDIMENTATION. 


IT  has  already  been  explained  in  the  intro 
duction  that  this  method  of  purification  con 
sisted  of  several  parts,  each  of  which,  to  quite 
a  degree,  was  distinct  in  its  nature  and  in  its 
application.  The  last  part  of  the  process  is 
the  passage  of  the  water  downward  through 
a  layer  of  sand  either  by  gravity  or  pressure, 
in  order  to  remove  from  the  water  the  bac 
teria,  aluminum  hydrate,  mud,  clay,  and  other 
suspended  matters. 

This  final  operation  is  properly  called  nitra 
tion.  It  is  erroneous,  however,  to  speak  of 
the  entire  process  as  filtration,  or  mechanical 
filtration,  because,  so  far  as  waters  like  the 
Ohio  River  are  concerned,  filtration  is  only 
one  of  several  steps  in  a  process  of  economical 
purification. 

This  (American)  type  of  filtration  differs  in 
several  respects  from  the  older  (English)  type 
of  filtration  which  has  been  adopted  and 
studied  in  Europe  and  several  places  in  this 
country.  There  are  two  chief  differences, 
namely: 

1.  In   American   filters  the  aluminum  hy 
drate  remaining  in  the  water  as  it  flows  from 
the  settling  chamber  to  the  filter,  by  virtue  of 
its  gelatinous  nature,  enveloping  the  bacteria 
and  other  suspended  matters,  makes  it  prac 
ticable  to  allow  the  water  to  pass  through 
the  sand  at  a  much  more  rapid  rate  than  in 
the  case  of  English  filters. 

2.  In  American  filters  the  accumulation  of 
matters  which  are  removed  from  the  water  by 
the  sand  (bacteria,  aluminum  hydrate,  mud, 
clay,  and  other  suspended  matters)  is  in  turn 
removed  from  the  sand  by  the  passage  of  a  re 
verse  current  of  water  through  the  sand  from 
the  bottom  to  the  top,  either  with  or  without 
accompanying  agitation  of  the  sand.       The 


corresponding  accumulations  in  English  fil 
ters  of  foreign  matter  from  the  water,  located 
for  the  most  part  at  and  near  the  surface  of  the 
sand,  are  removed,  practically  speaking,  by 
scraping  the  surface  of  the  sand  layer  with  a 
shovel  or  similar  implement  to  a  depth  ordi 
narily  of  0.5  inch  or  thereabouts. 

By  corresponding  accumulations  on  the 
sand  in  the  English  filters  is  meant,  ordina 
rily,  the  various  kinds  of  material  noted,  with 
the  exception  of  the  aluminum  hydrate;  al 
though  it  is  not  to  be  forgotten  that  aluminum 
hydrate,  formed  from  the  decomposition  of 
alum  added  to  river  water,  was  used  for  some 
years  in  I  lolland  in  connection  with  the  puri 
fication  of  public  water  supplies  by  English 
filters. 

The  systems  which  were  investigated  dur 
ing  these  tests  are  included  in  the  American 
type  of  filtration  and  are  all  divided  into  three 
main  divisions.  Each  division  includes  the 
devices  used  for  carrying  out  one  step  of  the 
process,  and  it  is  to  be  noted  that  it  was  only 
in  the  design  and  construction  of  these  de 
vices  that  these  systems  differed.  These  di 
visions  may  be  outlined  as  follows: 

1.  An    arrangement    for    the    preparation 
and  delivery  of  the  chemicals.     This  included 
preparation  tanks;  pumps  or  other  devices  for 
delivering  the  solutions  to  the  river  water; 
pipes  and  fittings;  valves  and  other  regulat 
ing  devices;  scales,  gauges,  hydrometers,  etc. 

2.  A  chamber  or  basin  for  the  reception  of 
the  treated  water  and  in  which  coagulation 
and  sedimentation  took  place  to  a  greater  or 
less  degree.     This  included  all  the  necessary 
inlet,  outlet,  and  drain  pipes,  and  the  devices 
used  for  controlling  the  flow  of  water  through 
the  basin. 


DESCRIPTION  Of    FILTERS. 


3.  A  filter  and  appurtenances.  This  division 
included  a  tank  which  contained  the  sand 
layer  and  water  to  be  hitered;  a  system  of 
strainers  for  removing  the  water  trom  the 
sand;  a  system  for  distributing  the  wash- 
water  beneath  the  sand  layer;  and,  in  the  case 
of  the  Warren  and  Jewell  systems,  a  set  of 
rakes  with  operating  mechanism  for  stirring 
the  sand.  All  piping,  valves,  and  regulating- 
devices  which  pertained  to  the  filter  are  in 
cluded  in  this  division. 

in  Chapter  11  the  devices  included  in  the 
first  division  have  been  described  in  consid 
erable  detail.  The  second  division  has  been 
presented  in  Chapter  IV,  and  it  now  remains 
to  present  the  third  division,  which  is  the  sub 
ject  of  this  chapter. 

In  the  next  chapter  will  be  found  a  sum 
mary  of  the  principal  parts  of  winch  each 
division  of  each  system  was  composed,  to 
gether  with  a  record  of  the  repairs,  changes, 
and  delays  noted  during  these  tests. 

The  manner  of  operation  of  these  systems 
is  given  in  Chapter  VT1,  where  a  more  com 
plete  description  of  the  special  regulating  de 
vices  is  also  presented. 

The  niters  of  the  respective  systems  are 
described  in  the  order  which  has  been  fol 
lowed  heretofore. 

All  elevations  used  are  in  feet  and  refer  to 
the  bottom  of  the  respective  sand  layers  as 
the  datum  plane.  The  accompanying  draw 
ings  will  facilitate  an  understanding  of  the 
several  niters  and  their  respective  appurte 
nances. 

THE  WARREN  FILTER  AND  APPURTENANCES. 

The  filter  was  placed  in  a  circular  wooden 
tank.  About  1.5  feet  from  the  bottom  was 
the  strainer  system,  which  was  made  of  per 
forated  copper  plates  with  suitable  wooden 
supports.  The  layer  of  sand  which  was  used 
as  a  filtering  medium  was  placed  upon  the 
strainer  system.  Above  the  sand  there  was  an 
'open  compartment  which  contained  the  water 
to  be  filtered.  During  filtration  the  water 
passed  by  gravity  from  the  upper  compart 
ment  through  the  sand  layer  and  strainer 
system  into  a  closed  compartment  situated 
between  the  strainer  system  and  the  bottom 
of  the  tank,  from  which  a  pipe  connected  with 


the  weir  box,  where  the  rate  of  filtration  was 
regulated.  For  washing,  the  water  was  re 
moved  from  the  upper  compartment  and 
wash-water  admitted  under  pressure  into  the 
lower  chamber,  from  which  it  forced  its  way 
up  through  the  sand.  After  passage  through 
the  sand  the  wash-water  was  removed  from 
the  upper  compartment  by  drain  pipes.  Dur 
ing  washing  the  sand  was  stirred  by  rakes 
which  were  supported  at  the  top  of  the  tank. 
Plans  and  sections  of  the  Warren  System  will 
be  found  on  Plates  II  and  111,  respectively. 

Filter  Tank. — The  filter  tank  was  made  of 
alternate  cypress  and  pine  staves,  the  bottom 
being  entirely  of  cypress.  It  was  10.6  feet  in 
diameter  on  the  inside  and  9.75  feet  deep 
inside.  The  staves  were  2.62  inches  thick  and 
6  inches  wide.  They  were  strongly  bound 
with  iron  hoops,  six  in  number.  The  hoops 
were  0.6  inch  thick  and  2  inches  wide. 

About  1.5  feet  from  the  bottom  of  the  tank 
were  wooden  pieces  which  served  as  a  support 
for  a  copper  strainer  floor.  In  the  open  com 
partment  above  the  perforated  copper  floor 
was  the  layer  of  sand.  The  closed  compart 
ment  beneath  the  copper  floor  was  the  fil- 
tered-water  chamber,  through  which  the  fil 
tered  water  passed  as  it  made  its  exit  from  the 
filter.  The  filtered  water  used  for  washing 
the  filter  also  passed  through  this  closed  com 
partment  as  it  was  pumped  upward  through 
the  sand. 

From  the  bottom  of  the  tank  a  central  well 
4.33  feet  in  height  extended  through  the  fil- 
tered-water  chamber,  strainer  floor,  and  the 
sand  layer.  For  a  distance  of  1.17  feet  from 
the  bottom  the  diameter  of  this  well  was  2.42 
feet,  and  above  this  point  1.71  feet. 

Across  the  top  of  the  tank"  lay  two  timbers, 
one  12  by  12  inches  and  the  other  6  by  12 
inches,  on  which  rested  the  bulk  of  the  ap 
pliances  for  the  operation  of  the  agitator. 
The  main  vertical  shaft,  to  which  the  rakes 
were  fastened,  was  supported  at  the  top  by 
these  timbers  and  guided  at  the  bottom  by  a 
casting  on  the  upper  end  of  the  central  well. 

The  height  of  water  above  the  sand  during 
filtration  was  normally  about  5.75  feet.  As 
described  beyond,  the  total  available  acting 
head  was  4.17  feet. 

The  above  description  in  general  terms 
shows  the  relation  to  each  other  of  the  vari- 


WATER  PURIFICATION  AT  LOUISVILLE. 


ous  devices  located  in  the  filter  tank.  The  de 
tails  of  these  devices  and  their  piping  con 
nections  are  as  follows: 

Inlet  Water-pipe. — The  main  inlet  water- 
pipe  was  8  inches  in  diameter  and  conducted 
the  \vater  by  gravity  from  the  outlet  of  the 
settling  basin.  This  pipe  led  into  and  across 
the  bottom  of  the  riltered-water  chamber,  at 
the  bottom  of  the  filter  tank,  and  connected 
with  the  central  well  by  a  flange  joint. 

Arrangement  for  the  Exit  of  the  Filtered 
Water. — After  passage  through  the  sand  the 
water  passed  through  the  strainer  system, 
composed  of  perforated  copper  plates  and 
wooden  supports;  next  through  the  filtered- 
water  chamber;  and  thence  through  an  8- 
inch  pipe  to  the  weir  box.  From  the  weir 
box  the  water  passed  through  about  65 
feet  of  5-inch  pipe  to  the  filtered-water  reser 
voir. 

Strainer  System. — The  original  strainer  sys 
tem  consisted  of  punched  copper  plates  sup 
ported  by  a  network  of  radial  and  circum 
ferential  wooden  braces.  Details  of  the  ar 
rangement  of  these  braces  can  best  be  under 
stood  by  an  examination  of  the  accompany 
ing  drawings  (Plates  II,  III,  VIII). 

The  radial  supports  were  2.25  by  2.75 
inches,  with  the  long  side  set  vertically.  They 
were  supported  at  the  center  on  a  shoulder 
made  for  that  purpose  in  the  central  well,  and 
at  the  periphery  on  a  ring  made  of  short 
wooden  sections  nailed  to  the  inside  of  the 
tank.  They  fitted  tightly  together  at  the  cen 
tral  well  and  were  7  inches  apart  at  the  pe 
riphery.  On  top  of  these  supports  was  laid  a 
second  set  of  ribs,  each  1.37  by  0.75  inches, 
with  the  long  side  set  vertically.  Between 
this  upper  set  of  ribs  were  laid  pieces  1.25  by 
0.75  inches,  set  perpendicular  to  the  radius  at 
their  center. 

These  circumferential  spacers  were  sup 
ported  at  each  end  by  the  main  radial  beams, 
and  were  level  on  top  with  the  upper  radial 
strips.  The  spacers  were  not  accurately  cir 
cumferential,  but  were  really  a  series  of  short 
chords. 

The  perforated  copper  plates  were  placed 
on  top  of  the  ribs  and  spacers,  and  were  fas 
tened  to  them.  They  were  made  in  sections 
of  the  size  of  the  space  subtended  by  the  radial 
ribs.  The  joints  of  the  plates  were  over  these 


ribs  and  were  protected  by  copper  strips  1.12 
inches  wide. 

Exit  Area. — The  orifice  area  of  the  copper 
plate  system  was  made  up  of  about  681,900 
punched  holes.  These  holes  averaged  0.043 
inch  (i.i  millimeter)  in  diameter.  They 
averaged  10.5  per  linear  inch  radially,  and  7.5 
per  linear  inch  at  right  angles  thereto. 

The  size  and  spacing  varied  considerably, 
but  the  above  figures  are  averages  of  numer 
ous  determinations  at  different  parts  of  the 
strainer  area.  Using  these  figures  as  a  basis 
of  computation,  the  total  orifice  area  of  the 
copper-plate  system,  including  all  holes  ex 
posed  on  the  upper  side,  was  1032  square 
inches.  No  possible  method  of  determining 
how  much  water  passed  through  the  holes 
directly  over  the  supports  was  found.  It 
seems  probable,  however,  that  the  weight  of 
the  sand  would  press  the  plates  sufficiently 
close  to  the  supports  to  obstruct  the  passage 
of  water  to  a  considerable  extent.  Deduct 
ing  all  such  holes,  the  net  area  was  923  square 
inches. 

On  April  12,  1896,  a  finer  sand  was  put  in 
service,  and  it  was  found  to  be  too  fine  to  use 
with  the  original  perforated  copper  plates  de 
scribed  above.  Accordingly  an  auxiliary 
strainer  device,  consisting  of  a  fine  brass 
gauze,  was  added.  This  gauze  was  laid  di 
rectly  over  the  copper  plates,  the  same  copper 
strips  being  used  to  keep  it  in  place.  Owing 
to  inability  to  secure  readily  a  sufficient  quan 
tity  of  gauze  of  the  desired  size  two  sizes  were 
used.  The  first  portion,  which  was  used  to 
cover  about  80  per  cent,  of  the  area,  had  65 
meshes  to  the  linear  inch.  For  the  remaining 
20  per  cent,  of  the  area  a  gauze  which  had 
80  meshes  per  linear  inch  was  used. 

By  the  introduction  of  the  brass  gauze  the 
determination  of  the  available  exit  area  of  the 
strainer  system  was  complicated.  There  were 
two  extreme  areas  which  may  be  considered, 
the  true  area  utilized  being  somewhere  be 
tween  the  two,  apparently. 

1 .  The  brass  gauze  may  be  assumed  to  have 
reduced  the  exit  area  of  the  perforated  copper 
plates.     In  this  case  the  gauze  is  assumed  to 
have  allowed  water  to  pass  through  only  those 
portions  of  it  which  were  directly  above  the 
holes  in  the  copper  plate. 

2.  It  may  be  assumed  that  the  entire  exit 


DESCRIPTION   OF  FILTERS. 


7.; 


area  of  the  holes  in  the  copper  plates  was 
available,  and  that  the  water  could  in  all  cases 
pass  more  or  less  freely  between  the  gauze 
and  the  copper  plates. 

The  second  supposition  appears  to  be  more 
nearly  correct,  because,  no  matter  how  closely 
the  gauze  was  pressed  upon  the  copper  plate, 
unless  the  wires  were  flattened,  innumerable 
channels  must  have  existed  through  which 
the  water  could  flow  more  or  less  freely. 

Filtered-water  Chamber. — Directly  beneath 
the  strainer  floor  and  forming  the  bottom  of 
the  filter  tank  was  a  closed  compartment 
which  was  used  as  a  collecting  chamber  for 
the  filtered  water,  and  also  as  a  distributing 
chamber  for  the  wash-water.  It  was  simply 
the  space  left  in  the  construction  of  the  tank, 
no  finishing  being  used. 

The  total  depth  of  the  chamber  was  1.5  feet, 
but  the  upper  part  was  largely  obstructed  by 
the  braces  of  the  strainer  floor,  below  which 
the  depth  was  i.i  feet. 

The  area  of  the  base  of  this  chamber  was 
somewhat  less  than  that  of  the  main  tank,  on 
account  of  restrictions  by  the  wooden  rim 
which  supported  the  outer  side  of  the  strainer 
floor  and  by  the  central  well.  The  area  was 
70.6  square  feet. 

The  total  capacity  of  the  chamber  was  94.7 
cubic  feet,  including  the  spaces  between  the 
supports  of  the  strainer  floor. 

The  chamber  could  be  drained  through  the 
waste-water  pipe  to  within  0.6  foot  of  the 
bottom.  No  arrangements  were  made  for 
complete  draining. 

A  small  hand-hole  was  provided  in  one  side 
of  the  tank  for  the  purpose  of  inspection. 

The  only  method  for  cleaning  was  by  forc 
ing  filtered  water  into  the  chamber  and  allow 
ing  it  to  flow  out  through  the  waste-water 
pipe. 

Weir  Box. — The  weir  box  was  an  open, 
rectangular  compartment  constructed  at  the 
northwest  corner  of  the  settling  basin,  and 
built  in  connection  therewith  of  the  same  ma 
terial.  It  was  connected  with  the  filtered- 
water  chamber  by  an  8-inch  pipe,  8  feet  in 
length. 

It  was  5.71  feet  long  by  2.75  feet  wide,  in 
side  dimensions.  The  weir  partition  ran 
across  the  short  dimension,  dividing  the  box 
into  an  inlet  and  an  outlet  side.  The  inlet  side 


was  2.67  by  2.75  feet,  and  the  outlet  3.04  by 
2.75  feet.  As  first  constructed  the  weir  was 
a  fixed  one  with  its  crest  approximately  at  an 
elevation  of  6.00  feet.  On  Nov.  25  it  was 
lowered  to  approximately  5.5  feet. 

With  other  changes  previous  to  Nov.  25 
a  movable  weir  was  inserted.  This  weir  was 
made  of  an  iron  plate  moving  in  guides  at  the 
sides,  its  position  being  controlled  by  a  worm 
shaft  operated  by  a  wheel  on  the  floor  over 
the  settling  basin.  It  had  an  available  ver 
tical  movement  from  an  elevation  of  3.85  to 
the  maximum  water  level  (elev.  8.02),  a  dis 
tance  of  4.17  feet.  The  nominal  crest  was  2.1 
feet  wide,  but  on  account  of  leakage  in  the 
guides  its  actual  width  was  probably  about  2.5 
feet. 

A  3-inch  valve  connecting  the  two  sides  was 
put  in  the  bottom  of  the  weir  box  Feb.  12 
to  allow  more  complete  draining  of  the  filter 
before  washing.  The  center  of  this  valve  was 
at  elevation  — 1.13.  From  the  weir  box  the 
water  flowed  through  about  65  feet  of  5-inch 
pipe  to  the  filtered-water  reservoir. 

Outlet  for  Filtered  Waste  Water. — At  such 
times  as  in  the  opinion  of  the  operator  the 
filtered  water  was  not  of  a  satisfactory  charac 
ter,  a  3-inch  pipe  leading  from  the  filtered- 
water  chamber  to  the  sewer  was  used  in  place 
of  the  main  outlet  through  the  weir  box. 

Sand  Layer. 

During  the  test  several  changes  were  made 
in  the  sand  layer,  the  kind  of  sand,  the  thick 
ness  of  the  layer,  and  the  area  of  the  surface, 
all  having  been  changed. 

Kinds  of  Sand  Used. — At  the  opening  of 
the  test  the  sand  layer  was  composed  of  sand 
No.  I.  This  was  removed  Jan.  22,  and  sand 
No.  2  put  in  place  and  used  up  to  April  13. 
On  April  17  sand  No.  3  was  put  in  place. 
This  was  used  up  to  July  25,  when  2  inches  of 
sand  containing  23  parts  of  No.  3  and  one 
part  of  a  very  fine  sand  were  added.  No.  i 
was  natural  sand;  the  other  two  were  crushed 
quartz.  Mechanical  analyses  of  these  sands 
gave  results  which  are  presented  on  the  next 
page. 

Thickness  of  Sand  Layer. — The  thickness 
of  the  sand  layer  varied  from  three  causes: 

i.  Addition  of  sand  by  the  operators  of  the 
filter. 


74 


WATER   PURIFICATION  AT  LOUISVILLE. 


MECHANICAL   ANALYSES   OF   THE   SANDS  USED 
IN    THE   WARREN    FILTER. 


Finer  than  2.04    millimeters... 

"      0.93 

"     0.462 
"         "     0.316  " 

"     0.182 

.-._      .       (Ten  per  cent  finer  than  ) 
Effective  J      dia^eter  in   miilime-  ' 


100. 

100. 
4-2 

0.3 

O.  I 


ent.  by  > 
100. 
IJ.O 
0.2 


eight. 
IOO. 

95.5 

6.5 
0.9 


0.56 


2.  Losses  of  some  of.  the  finer  portions  of 
the  sand  during  the  process  of  washing. 

3.  Increased  compactness  of  the  sand  layer. 
At  different  places  on  the  surface  of  the 

sand  layer  the  thickness  varied  owing  to  the 
action  of  the  rake-teeth  of  the  agitator.  As 
the  agitator  revolved  during  washing  a  small 
portion  of  the  sand  was  moved  from  the  cen 
tral  part  of  the  layer  towards  the  periphery. 
The  effect  of  this  action  was  cumulative.  Ob 
servations  made  on  Jan.  20,  Feb.  14,  April  13, 
May  22,  and  July  17  showed  differences  in 
the  elevations  of  the  surface  of  the  layer  at 
the  central  well  and  at  the  periphery,  ranging 
from  i  to  4  inches. 

On  Nov.  25,  1895,  the  average  thickness 
of  the  sand  layer  was  about  2.36  feet.  This 
thickness  was  increased  on  Jan.  3,  1896,  by 
the  addition  of  0.6  inch  of  new  sand  (No.  i). 

The  average  thickness  of  the  layer  of  sand 
No.  2  on  Jan.  25  was  1.86  feet.  On  Feb.  12 
this  thickness  was  increased  to  2.25  feet. 

With  the  third  lot  of  sand  the  thickness  of 
the  layer  when  new,  April  17,  was  2.17  feet; 
on  May  22,  2.12  feet;  and  on  July  17,  2.00 
feet. 

On  July  25,  0.25  foot  of  mixed  sand  was 
added. 

The  average  thickness  at  the  close  of  the 
test  was  2.25  feet. 

Area. — As  first  arranged  the  sand  layer 
extended  to  the  wall  of  the  filter  tank  and  the 
surface  area  of  the  sand  was  equal  to  the  area 
of  the  filter  tank,  excepting  the  central  well. 
1.8  feet  in  diameter.  This  area  was  approxi 
mately  85.70  square  feet.  Practically  all  of 
the  tests  were  made  after  the  completion  on 
Nov.  25  of  a  new  collecting  gutter  to  carry 
the  wash-water  to  the  sewer-pipe.  This  made 
the  diameter  of  the  sand  layer  10.1  feet  includ 
ing  the  central  well  above  noted. 

Allowing  2  square  inches  for  each  of  ifi 
teeth  which  extended  into  the  sand  bed  dur 


ing  filtration,  the  net  area  of  the  surface  of  the 
sand  was  77.36  square  feet. 

From  April  17  to  July  25  the  rake-teeth 
barely  pierced  the  sand  layer,  thus  increasing 
the  area  to  77.50  square  feet. 

Device  for  Cleaning  the  Sand  Layer. 

The  device  for  cleaning  the  sand  layer  by 
washing  comprised  the  following  principal 
parts  which  are  described  in  turn  below: 

1.  Pipes  through  which  filtered  water  was 
pumped  from  the  filtered-water  reservoir  into 
the     filtered-water     chamber,     and     thence 
through  the  strainer  system  into  the  bottom 
of  the  sand  layer. 

2.  Auxiliary  slotted  pipes,  located  at  the 
bottom    of   the    sand    layer   just    above   the 
strainer  system,  through  which  for  a  short 
time  part   of  the  wash-water  was   pumped, 
with  the  view  to  getting  more  uniform  dis 
tribution. 

3.  A  collecting  gutter  and  pipes  to  carry 
to  the  sewer  the  last  portion  of  the  water  on 
the  sand  layer  just  after  draining  the  filter 
prior  to  washing,  and  the  wash-water  after  it 
had  passed  through  the  sand  layer. 

4.  An  agitator  with  the  necessary  mechan 
ism  for  stirring  the  sand  during  the  process 
of  washing. 

5.  An   engine,   with   pulleys,   belting,   and 
shafts,  to  operate  the  agitator. 

Wash-water  Supply  Pipe. — The  wash-water 
taken  from  the  filtered-water  reservoir  was 
pumped  through  an  8-inch  pipe.  This  ar 
rangement  was  used  by  all  the  filters  in  com 
mon.  From  the  pump  to  a  point  on  this  pipe 
where  a  separate  pipe  branched  to  the  Warren 
System  was  about  100  feet;  a  4-inch  pipe  TO 
feet  in  length  led  from  this  point  to  the  fil 
tered-water  chamber  beneath  the  sand.  At 
first  a  3-inch  valve  was  located  on  this  pipe 
just  outside  the  filter  tank. 

With  this  3-inch  valve  on  the  4-inch  pipe 
the  distribution  of  wash-water  was  not  satis 
factory.  The  restriction  in  the  pipe  caused  by 
the  small  valve  gave  something  of  a  nozzle 
effect,  so  that  the  stream  of  water  entered 
the  filtered-water  chamber  with  sufficient 
velocity  to  strike  the  outer  wall  of  the  central 
well,  and  be  deflected  up  through  a  compara 
tively  small  area  of  the  strainer  svstem  and 


DESCRIPTION  OF  F I  HERS. 


75 


of  the  sand  layer.  To  remedy  this  difficulty, 
and  to  increase  the  loss  of  pressure  in  the 
piping,  the  3-inch  valve  was  replaced  on  Feb. 
12  by  a  4-inch  valve. 

Auxiliary  Slotted  Pipes  for  the  Distribution 
of  Wash-water. — In  addition  to  putting  a 
larger  valve  on  the  wash-water  pipe  on  Feb. 
12,  there  were  also  introduced  at  the  same 
time  supplementary  pipes  to  convey  a  portion 
of  the  wash-water  to  different  points  at  the 
bottom  of  the  sand  layer. 

A  2-inch  brass  pipe  branched  from  the  main 
wash-water  supply  just  outside  the  filter  tank, 
the  flow  being  regulated  by  a  2-inch  valve. 
This  pipe  entered  the  tank  above  the  perfo 
rated  copper  floor  on  which  the  sand  rested. 
It  connected  directly  with  a  ring  of  2-inch  iron 
pipe  made  of  tees  and  eighth  bends. 

The  water  was  distributed  by  six  i-inch 
slotted  tubes  of  brass  and  the  inlet  pipe  noted 
above,  which  was  also  slotted.  The  seven 
pipes  or  tubes  were  laid  radially,  spaced 
equally  around  the  central  well,  and  fitted  into 
the  respective  tees  in  the  iron  ring  encircling 
the  central  well. 

Two  rows  of  longitudinal  slots  90°  apart 
extended  the  entire  length  of  each  tube. 
They  averaged  2  inches  in  length,  0.031  inch 
in  width,  and  were  approximately  3  inches 
apart.  All  of  the  tubes  were  capped  at  the 
ends,  and  in  the  center  of  each  cap  was  a  hole 
0.031  inch  in  diameter.  The  tubes  were  first 
set  with  the  slots  on  the  under  side,  with  the 
center  of  the  tube  2.25  inches  above  the  per 
forated  copper  bottom  at  the  inner  end  and 
3  inches  above  at  the  outer  end. 

On  Feb.  19  the  tubes  were  reversed,  bring 
ing  the  slots  on  the  upper  side.  The  entire 
device  was  removed  on  Feb.  21. 

Collecting  Gutter  and  Central  Well. — The  cir 
cular  collecting  gutter  was  constructed  of 
wood  and  galvanized  sheet  iron.  A  lining  of 
pine  staves  0.25  foot  thick,  extending  from 
the  strainer  floor  to  2.35  feet  above  it,  was 
placed  inside  the  filter  tank.  On  the  side  of 
the  lining  towards  the  inner  well  a  strip  of 
galvanized  iron  was  tacked,  its  upper  edge 
extending  0.5  foot  above  the  staves.  The 
space  thus  formed  between  the  metal  strip 
and  the  main  wall  of  the  tank  was  used  as  a 
gutter.  The  upper  edge  of  the  metal  strip, 
or,  in  other  words,  the  discharge  level,  was  at 


elevation  2.85  feet.  At  three  equidistant 
points  collections  were  made  with  this  gut 
ter  to  a  3-inch  pipe  which  partially  encircled 
the  filter  tank  on  the  outside. 

This  3-inch  pipe  connected  by  means  of  a 
special  casting  with  a  branch  from  the  inlet 
pipe  from  the  settling  basin  to  the  filter, 
which  in  turn  connected  with  the  sewer. 

By  means  of  a  tee  and  suitable  valves  on  the 
6-inch  inlet  pipe  to  the  filter,  this  pipe  was 
connected  with  the  sewer,  thus  allowing  the 
use  of  the  central  well  (1.8  feet  in  diameter) 
for  the  removal  of  unfiltered  waste  and  wash 
water. 

During  the  tests  the  crest  of  the  central 
well  was  changed  three  times.  When  the 
depth  of  the  sand  was  increased  on  Feb.  12 
the  height  of  the  well  was  also  increased  about 
4  inches.  It  was  lowered  again  on  Feb.  14 
to  the  original  height  in  order  to  try  the  effect 
on  the  sand  of  discharging  all  the  water  dur 
ing  washing  through  the  well.  On  Feb.  21 
it  was  raised  to  the  same  level  as  the  crest  of 
the  collecting  gutter. 

Agitator. — The  agitator  consisted  essen 
tially  of  two  horizontal  rake-arms  with  eight 
teeth  each,  and  the  necessary  mechanism  to 
raise  and  lower  the  rakes,  and  to  revolve  them 
as  desired.  Power  was  furnished  by  a  small 
engine,  and  transmitted  by  a  6-inch  belt  to  a 
counter-shaft,  from  which  another  belt  6 
inches  wide  led  to  the  driving  pulley  of  the 
mechanism.  For  simplicity  in  presentation  a 
general  description  of  the  operating  mechan 
ism  is  given,  referring  to  each  of  the  parts  by 
serial  numbers.  Following  this,  the  several 
parts  are  tabulated,  and  their  leading  dimen 
sions  given. 

The  rake-arms  were  hung  on  the  main  ver 
tical  shaft,  which  was  supported  at  the  upper 
end  by  the  frame  of  the  machine,  and  guided 
at  the  lower  end  by  a  collar  on  the  top  of  the 
inlet  well.  This  shaft  was  turned  around  by 
means  of  a  large  bevel  gear  (i),  a  lug  on 
which  fitted  into  a  vertical  slot  in  the  shaft. 
By  this  arrangement  the  shaft  could  be  raised 
or  lowered  without  interfering  with  the  rotary 
motion.  To  drive  the  gear,  a  pinion  (2)  on 
the  shaft  which  carried  the  main  driving  pul 
ley  drove  a  gear  (3)  on  a  lower  parallel  hori 
zontal  shaft.  At  the  end  of  this  shaft  was  a 
bevel  pinion  (4)  which  drove  the  rotating 


WA1ER  PURIFICATION  AT  LOUISVILLE, 


gear.  It  will  be  noticed  that  this  arrange 
ment  necessitated  rotation  of  the  main  verti 
cal  shaft  with  its  rakes  whenever  any  part  of 
the  mechanism  was  in  operation.  For  raising 
or  lowering  the  main  vertical  shaft,  power  was 
transferred  by  gearing  from  the  horizontal 
driving  shaft  to  an  upper  parallel  shaft,  on 
the  end  of  which  a  bevel  pinion  (5)  drove  the 
raising  and  lowering  gears.  For  transferring 
the  power  two  duplicate  sets  of  gears  con 
nected  the  main  driving  shaft  with  the  upper 
shaft.  Either  of  these  sets  could  be  used  as 
desired,  or  they  could  both  be  out  of  opera 
tion,  hand  levers  controlling  their  position. 
Each  set  consisted  of  the  driving  gear  (6); 
two  idle  gears  (7)  and  (8),  and  the  driven  gear 
(9);  (6)  and  (9)  were  the  same  for  both  sets, 
and  (7)  and  (8)  duplicates  in  each  set.  in  the 
original  machine  gear  (8)  was  omitted,  the  in 
creased  length  of  vertical  motion  of  the  modi 
fied  machine,  with  its  necessitated  increase  in 
height  of  the  frame,  requiring  the  introduc 
tion  of  the  second  gear. 

The  raising  and  lowering  gear  proper  con 
sisted  of  a  large  bevel  gear  (10),  and  a  sleeve 
on  the  main  shaft.  This  sleeve  was  made  of 
babbitt  metal  cast  on  the  main  vertical  shaft 
in  the  following  manner:  In  the  upper  end 
of  the  main  shaft  (the  lower  end  of  which 
held  the  rake-arms)  were  cut  nine  circular 
slots,  each  I  inch  wide  and  0.35  inch  deep. 
The  first  one  was  1.5  inches  from  the  top  of 
the  shaft.  Below  this  the  slots  were  spaced 
2.5  inches  apart.  On  the  shaft  thus  prepared 
was  cast  a  sleeve  of  babbitt  metal  0.75  inch 
thick  and  25  inches  long.  In  casting,  a  ver 
tical  slot  1.5  inches  wide  and  0.5  inch  deep 
was  left  in  this  sleeve.  This  slot  engaged  a 
lug  on  the  framework  of  the  machine,  and 
prevented  rotation  of  the  sleeve,  the  steel 
core  (main  shaft)  rotating  within  the  sleeve. 
On  the  face  of  the  sleeve  a  helical  thread  was 
cut,  with  three  threads  to  the  inch;  this  formed 
the  worm,  which  engaged  and  was  driven  by 
a  similar  thread  on  the  inside  of  the  lifting 
gear,  that  worked  freely  on  a  loose  bearing 
plate.  As  above  described,  a  bevel  pinion  on 
an  upper  horizontal  shaft  drove  this  gear. 

For  the  purpose  of  stopping  the  vertical 
motion  of  the  main  shaft  automatically,  lugs 
were  provided  on  the  vertical  shaft,  which 
at  the  limits  of  motion  (top  or  bottom)  oper- 


aied  sets  of  levers,  which  disengaged  the  set 
of  idle  gears  which  were  in  operation,  trans 
ferring  power  from  the  driving  shaft  to  the 
upper  parallel  shaft. 

The  main  dimensions  of  the  gears  and  pin 
ions  numbered  in  the  above  description  are  as 
follows: 

1.  Bevel  gear,  35  inches  in  diameter  with 
72  teeth. 

2.  Pinion,  5.75  inches  in  diameter  with  14 
teeth. 

3.  Gear,   26   inches   in   diameter   with   50 
teeth. 

4.  Bevel  pinion,  with  13  teeth. 

5.  Bevel  pinion,  with  15  teeth. 

6.  Gear,  4.25  inches  in  diameter  with  24 
teeth. 

7.  Gear,  6.25  inches  in  diameter  with  36 
teeth. 

8.  Gear,  8.25  inches  in  diameter  with  48 
teeth. 

9.  Gear,  8.25  inches  in  diameter  with  48 
teeth. 

10.  Bevel   gear,    16.5   inches   in   diameter 
with  66  teeth. 

Rakes. — Attached  by  means  of  a  collar  and 
socket  bolts  to  the  main  vertical  shaft  were 
the  rake-arms.  These  were  two  in  number 
and  were  set  180°  apart.  Two  shorter  arms 
on  the  other  diameter  carried  tie-rods  to 
strengthen  the  rake-arms.  The  rake-teeth 
were  of  cast  iron.  The  original  teeth  were 
27  inches  long,  but  later  a  change  was  made, 
and  35-inch  teeth  were  inserted.  There  were 
eight  teeth  on  each  arm.  They  were  wedge- 
shaped  in  section,  the  back  being  rounded. 
On  the  original  teeth  a  wedge-shaped 
shoulder  was  cast  13.25  inches  from  the  upper 
part  of  the  teeth.  This  was  not  used  in  the 
longer  teeth. 

As  first  used,  the  rakes  in  the  upper  position 
were  clear  of  the  sand,  and  in  the  lower  posi 
tion  they  averaged  5  inches  from  the  strainer 
floor.  On  Feb.  21  they  were  lowered  so  that 
they  came  within  2  inches  of  the  floor,  longer 
rakes  being  introduced  at  the  same  time  to 
allow  for  this  greater  penetration.  The  lift 
of  the  original  machine  was  found  to  be  too 
small  with  this  new  arrangement  to  raise  the 
rake-teeth  clear  of  the  sand;  and  on  April  13 
a  new  machine  was  put  in  service  as  noted 
above,  giving  approximately  8  inches  greater 


DESCRIPTION  OF  FILTERS. 


77 


lift  of  the  rakes.  At  the  close  of  the  test  with 
the  sand  layer  27  inches  thick,  the  rake-teeth 
remained  about  i  inch  in  the  sand  at  the 
upper  position. 

Engine  and  Belting. — The  engine  was  a 
Carlisle  single-cylinder,  fly-wheel  engine.  The 
size  was  5.75  by  6  inches,  with  77  per  cent, 
cut-off.  The  engine  drove  a  6-inch  belt  over 
a  12-inch  pulley  8.25  inches  wide. 

From  the  engine  a  6-inch  rubber  belt  drove 
a  2O-inch  pulley  on  a  2.5-inch  counter-shaft. 
Another  6-inch  belt  from  a  1 6-inch  pulley  on 
the  counter-shaft  drove  an  1 8-inch  pulley  on 
the  agitator  machinery. 

Elevations. 

The  different  elevations  in  feet,  referred  to 
the  bottom  of  the  sand  layer  as  the  datum 
plane,  were  as  follows: 

Bottom  of  sand  layer  (top  of  strainer 

floor) o.oo 

Floor  of  filtered-water  chamber -  1.48 

Sand  surface  (average,  Aug.  i,  1896).   +2.27 
Crest  of  central  well  and  circular  gut 
ter  +  2.85 

Lower  end  of  rake-teeth  (agitator  up) .   +  1.94 

Top  of  filter  tank +  8.27 

Average  maximum  water  level +  8.02 

Lower  floor  (main-house  floor) -  1.77 

Center  of  inlet  pipe  at  filter -  0.94 

Center  of  outlet  pipe  at  filter -0.85 

Center  of   wash-   and    waste-pipes   at 

•  filter -  0.98 

Lowest  position  of  weir +  3.85 

Highest  position  of  weir  (available  as 

outlet  +  8.02 

Crest  of  outlet  channel  from  settling 

basin  (mudsill) +  6.72 

THE  JEWELL  FILTER  AND  APPURTENANCES. 

The  layer  of  sand  forming  the  filtering 
medium  was  held  in  a  wooden  tank  set  in  the 
upper  compartment  of  the  main  tank.  The 
roof  of  the  settling  chamber  served  as  a  sup 
port  for  a  layer  of  bricks  and  cement  which 
covered  the  strainer  manifold,  and  formed  a 
support  for  the  sand  layer.  Between  the  inner 
and  outer  tanks  was  a  space  which  was  used 
as  a  collecting  gutter  for  draining.  A  central 


well  connected  the  compartment  above  the 
sand  with  the  settling  chamber.  During  fil 
tration  the  water  passed  downward  through 
the  sand  and  the  strainer  system  by  gravity. 
The  total  available  acting  head  was  about  14 
feet,  of  which  5.5  feet  were  positive  (above  the 
bottom  of  the  sand  layer),  and  8.5  negative. 
Plans  and  sections  of  this  system  are  shown 
on  Plates  IV  and  V,  respectively.  The  rate 
of  filtration  was  regulated  by  valves  on  the 
pipe  from  the  strainer  system.  When  the 
filter  required  washing,  the  water  in  the  com 
partment  above  the  sand,  about  2.5  feet  deep, 
was  removed  and  wash-water  admitted  to  the 
strainer  system  under  pressure.  Wash-water 
was  then  forced  up  through  the  sand  and  dis 
charged  into  the  space  between  the  two  tanks, 
from  which  it  was  removed  to  the  sewer. 
During  washing  the  sand  was  stirred  by  a  set 
of  rakes  supported  by  beams  at  the  top  of  the 
main  tank. 

Filter  Tank. — The  filter  tank  was  of  cypress, 
12.15  ^eet  m  inside  diameter,  5.0  feet  high  on 
the  outside,  and  3.41  feet  deep  above  the 
strainer  floor.  It  was  made  of  3-inch  staves 
and  was  strongly  bound  by  three  hoops,  each  3 
inches  wide  and  0.125  mcri  thick.  At  its  bot 
tom,  the  space  between  the  filter  tank  and  the 
main  tank  (about  0.3  foot  wide)  was  filled  by 
a  wooden  ring  0.33  foot  thick.  This  ring 
served  to  brace  the  bottom  of  the  staves,  and 
also  prevented  any  lateral  movement.  There 
was  no  floor  in  this  tank,  the  staves  resting 
upon  the  roof  of  the  settling  chamber.  The 
spaces  between  the  pipes  of  the  strainer  sys 
tem  were  filled  with  a  layer  of  brick  and 
cement,  supported  by  the  roof  of  the  settling 
chamber.  This  brick  and  cement  layer  in 
turn  supported  the  sand. 

The  strainer  system,  consisting  of  a  set  of 
pipes  to  collect  the  water  from  the  cups,  and 
cups  through  which  the  water  passed  from 
the  sand  layer,  was  laid  on  the  roof  of  the 
settling  chamber,  and  covered  by  the  layer  of 
bricks  and  cement,  the  face  of  which  was  flush 
with  the  top  of  the  strainer  cups. 

The  set  of  parallel  pipes  were  all  connected 
to  a  special  cast-iron  pipe  which  ran  across 
the  filter  tank.  On  one  side  this  casting  was 
connected  by  a  suitable  joint  with  the  outlet 
pipe.  This  pipe  conveyed  the  water  to  the 
outside  of  the  main  tank,  where  it  connected 


WATER   PURIFICATION  AT  LOUISVILLE. 


with  a  cross,  which  was  also  connected  to  the 
outlet  pipe  leading  to  the  nltered-water  res 
ervoir;  to  the  waste-water  pipe  leading  to  the 
sewer;  and  the  wash-water  supply  pipe.  A 
central  well  extended  from  the  settling  cham 
ber  through  the  strainer  floor  and  the  sand 
layer  to  about  1.4  feet  above  the  sand. 

At  the  top  of  the  main  tank  were  two  tim 
bers,  on  which  rested  the  bulk  of  the  appli 
ances  for  the  operation  of  the  agitator.  These 
timbers  were  supported  at  either  end  by  suit 
able  iron  brackets  fastened  on  the  inside  of 
the  wall  of  the  main  tank,  the  upper  face  of 
the  timbers  being  flush  with  the  top  of  the 
main  tank.  Ordinarily  the  water  above  the 
sand  layer  partly  submerged  these  timbers. 
The  main  vertical  shaft,  to  which  were  fast 
ened  the  rake-arms  of  the  agitator,  was  sup 
ported  at  the  top  by  these  timbers,  and  guided 
at  the  bottom  by  a  ring  on  the  inlet  well. 

The  above  description  in  general  terms 
shows  the  relation  to  each  other  of  the  various 
devices  located  in  the  filter  tank.  The  details 
of  these  devices  and  the  piping  connections 
were  as  follows: 

Inlet  Water-pipe. — The  inlet  water-pipe  was 
a  central  well  0.67  foot  in  diameter  and  4.5 
feet  high.  It  was  made  of  cast  iron. 

Arrangements  for  the  Exit  of  the  Filtered 
Water. — After  passage  through  the  sand  the 
water  passed  through  the  strainer  system, 
consisting  of  444  strainer  cups  and  suitable 
collecting  pipes,  to  a  connection  with  a  5-inch 
pipe.  This  pipe  connected  with  a  cross  out 
side  the  filter.  From  the  cross  there  were 
about  8  feet  of  4-inch  pipe  leading  to  the  au 
tomatic  controller,  from  which  about  65  feet 
of  5-inch  pipe  led  to  the  filtered-water  reser 
voir. 

Strainer  System. — The  strainer  system  con 
sisted  of  brass  strainer  cups  screwed  into  a  set 
of  collecting  pipes.  The  shape  and  size  of 
these  cups,  of  which  there  were  444,  is  shown 
on  the  drawings.  The  face  of  the  cup  was 
covered  with  a  punched  aluminum  bronze 
plate,  the  plate  being  secured  to  the  cup  by  a 
ring  which  was  riveted  to  the  cup  flange.  The 
strainer  cups  were  screwed  directly  into  the 
collecting  pipes,  the  arrangement  of  which  is 
shown  on  the  drawings. 

A  central  casting  was  fastened  to  the  filter 
floor  by  six  o.75-inch  studs.  In  general  form 


this  casting  was  a  hollow  annular  ring  with 
flange  joints  on  two  ends  of  one  diameter. 
To  each  of  these  flanges  was  attached  a  length 
of  5-inch  pipe,  each  length  being  made  in 
three  sections  2  feet,  i  foot,  and  2  feet  long, 
respectively.  The  central  section  in  one  side 
was  a  nipple,  and  in  the  other  a  tee  with  the 
short  arm  passing  down  through  the  filter 
floor.  The  outlet  pipe  connected  to  this  arm. 
Running  from  the  5-inch  pipes  above  de 
scribed,  and  also  from  the  central  casting,  was 
a  system  of  i. 5-inch  pipes,  23  on  each  side  of 
the  large  pipes.  These  pipes  were  of  different 
lengths  to  fit  the  inner  circumference  of  the 
filter  tank.  The  shortest  was  1.33  feet  and 
the  longest  5.0  feet.  They  were  spaced  0.5 
foot  from  center  to  center.  All  of  the  pipes 
were  capped  at  the  ends.  The  strainer  cups 
were  screwed  into  the  tops  of  the  whole  sys 
tem  as  above  described;  six  in  the  central 
casting,  twenty  in  each  of  the  large  pipes,  and 
the  remainder  in  the  smaller  pipes.  These  cups 
were  all  spaced  approximately  6  inches  from 
center  to  center  except  in  the  central  casting. 
The  distribution  was  very  uniform;  the  great 
est  distance  from  any  cup  to  the  nearest  other 
cup,  or  from  any  point  on  the  floor  to  the 
nearest  cup,  was  6  inches.  The  shortest  dis 
tance  between  any  two  cups  (4  inches)  was 
at  the  central  casting. 

Exit  Area. — The  diameter  of  the  opening 
of  the  strainer  cups  was  1.69  inches,  and  the 
area  2. 24  square  inches.  The  aluminum  bronze 
plate  was  punched  with  twenty  holes  to  the 
linear  inch,  the  holes  averaging  0.028  inch 
(0.70  millimeter)  in  diameter  and  0.0006 
square  inch  in  area.  The  orifice  area  per  single 
strainer  cup  was  therefore  0.54  square  inch, 
giving  a  total  area  for  the  entire  system  of 
240  square  inches. 

The  passage  through  the  neck  of  the 
strainer  cup  was  0.188  inch  in  diameter.  The 
total  area  of  the  whole  system  was  12.26 
square  inches,  equivalent  to  a  small  fraction 
less  than  that  of  a  4-inch  pipe. 

The  major  portion  of  the  strainer  system 
was  covered  with  cement,  the  space  between 
the  pipes  being  filled  with  bricks.  This 
formed  the  filter  floor.  It  was  level  in  the 
main,  and  flush  with  the  top  of  the  strainer 
cups.  Where  the  cups  were  set  into  the  large 
pipes  and  central  casting  they  were  1.8  inches 


DESCRIPTION  OF  FILTERS. 


79 


higher  than  where  set  into  the  small  pipes. 
There  was  no  cement  over  the  large  pipes  or 
central  casting. 

Outlet  Pipe. — The  outlet  pipe  was  a  5-inch 
cast-iron  pipe  connected  to  the  short  arm  of 
the  tee  in  the  main  pipe  of  the  strainer  system. 
It  was  made  up  of  6.2  feet  of  straight  pipe  set 
vertically,  a  U  trap  and  a  length  of  5-inch 
horizontal  pipe  connecting  with  a  5-inch  cross 
outside  the  main  tank.  The  whole  length 
was  about  11.5  feet  to  the  center  of  the 
cross. 

From  the  cross  about  8  feet  of  4-inch  pipe 
connected  with  the  automatic  controller. 
The  filtered-water  meter  was  located  on  this 
pipe. 

Automatic  Controller. — The  automatic  con 
troller  consisted  of  a  galvanized-iron  tank,  set 
vertically,  open  at  the  top,  and  arranged  with 
a  sharp-edge  orifice  at  the  bottom;  an  ar 
rangement  of  the  outlet  piping  to  discharge 
into  the  top  of  this  tank;  a  funnel  under  the 
tank,  on  top  of  the  pipe  to  the  filtered-water 
reservoir,  to  collect  the  discharge  from  the 
orifice;  a  butterfly  valve  on  the  outlet  pipe 
above  the  tank;  a  balance  arm,  operating  the 
butterfly  valve,  one  end  of  the  arm  supporting 
a  weight,  the  other  a  copper  can;  and  a  con 
nection  from  the  base  of  the  tank  with  an  ad 
justable  overflow  which  discharged  into  the 
can  on  the  balance  arm.  The  device  was  de 
pendent  on  the  rate  of  overflow  into  the  can 
on  the  balance  arm,  an  increase  in  height  of 
water  in  the  main  tank  increasing  the  over 
flow,  thus  increasing  the  amount  of  water  in 
the  small  can,  which  caused  a  movement  of 
the  balance  arm  and  a  consequent  closing  of 
the  valve. 

A  4-inch  pipe  connected  with  the  outlet 
pipe  just  before  the  latter  reached  the  con 
troller.  It  was  used  when  the  necessary  act 
ing  head  fell  below  that  available  with  the 
controller.  This  pipe  emptied  into  the  sewer. 

From  the  controller  the  water  flowed  by 
gravity  through  about  65  feet  of  5-inch  pipe, 
emptying  into  the  filtered-water  reservoir  in 
side  the  house  for  the  wash-water  pump. 

Outlet  for  Filtered  Waste  Water. — A  4-inch 
pipe  connected  with  the  cross  above  men 
tioned  and  conveyed  such  water  as.  in  the 
opinion  of  the  operator,  was  not  of  a  satisfac 
tory  character  directly  to  the  sewer. 


Sand  Layer. 

During  the  test  the  sand  was  changed 
twice.  The  area  and  thickness  were  modified 
somewhat  during  the  test  by  changes  in  the 
tank  itself,  due  to  warping. 

Kinds  of  Sand  Used. — At  the  beginning  of 
the  test  the  sand  layer  was  composed  of  sand 
No.  4.  On  Feb.  i  this  was  removed  and  sand 
No.  5  put  in  its  place.  This  was  used  till 
July  3.  Sand  No.  13  was  put  in  service  July 
6  and  used  for  the  remainder  of  the  test.  Sand 
No.  13  was  a  natural  sand;  the  other  two 
were  crushed  quartz.  Mechanical  analyses  of 
these  sands  gave  the  following  results: 

MECHANICAL   ANALYSES  OF  THE    SANDS   USED 
IN   THE   JEWELL   FILTER. 

No.  4.       No.  5.     No.  13. 
Per  cent,  by  weight. 

Finer  than  2.04   millimeters 100.0     100.0     100.0 

"     0.93  "          74.2       91.0       95.5 

"         "    o .  462  "  19.5       1 1 .  o       1 6 . 6 

0.316  "          1.4         1.4         1.4 

0.42       0.45       0.43 

Thickness  of  Sand  Layer. — The  thickness  of 
the  sand  layer  varied  slightly,  due  to  increased 
compactness  during  use  and  slight  wastes 
during  washing.  The  nominal  thickness  was 
34  inches.  On  Feb.  28  it  averaged  34  inches. 
On  July  6  the  new  sand  layer  was  reported  as 
34  inches  thick,  but  a  measurement  on  July 
8  gave  only  32  inches.  The  thickness  at  the 
close  of  the  test  was  30.5  inches. 

The  sand  layer  was  quite  uniformly  level, 
only  0.25  inch  difference  having  been  re 
corded  between  the  center  and  the  periphery. 
During  reverse  motion  the  rake-arms  cut  fur 
rows  in  the  surface  varying  in  depth  from 
0.25  to  0.75  inch.  The  impact  of  the  water 
over  the  crest  of  the  inlet  well  also  caused  a 
slight  depression  at  about  i  foot  from  the 
well.  The  rake-arms,  during  filtration,  pene 
trated  the  surface  of  the  sand  layer  from  3 
to  5  inches. 

Area. — An  average  of  several  determina 
tions  gave  115.8  square  feet  as  the  area  of  the 
sand  surface. 

Device  for  Cleaning  the  Sand  Layer. 

The  device  for  cleaning  the  sand  by  wash 
ing  comprised  the  following  principal  parts, 
which  are  described  in  turn  below; 


8o 


WATER   PURIFICATION  AT  LOUISVILLE. 


1.  Pipes  through  which  filtered  water  was 
pumped  from  the  filtered-water  reservoir  into 
the  outlet  piping  system. 

2.  The  strainer  system  already  described, 
which  was  used  as  a  system  for  the  distribu 
tion    of    the    wash-water    beneath    the    sand 
layer. 

3.  A  collecting  channel  to  convey  to  the 
sewer   the    wash-water    after    it    had    passed 
through  the  sand. 

4.  An  agitator  with  the  necessary  mechan 
ism  for  stirring  the  sand  during  washing. 

5.  An  engine  to  drive  the  main  shaft. 
Wash-water  Supply  Pipe. — The  wash-water 

taken  from  the  filtered-water  reservoir  was 
pumped  through  an  8-inch  pipe.  From  the 
pump  to  the  point  where  a  separate  pipe 
branched  to  the  Jewell  and  Western  systems 
was  about  60  feet.  From  this  point  10  feet 
of  5-inch  pipe  led  to  a  point  where  a  separate 
pipe,  made  up  of  about  4  feet  of  5-inch  pipe, 
a  meter,  and  about  3  feet  of  4-inch  pipe,  led 
to  a  connection  outside  the  main  tank. 

Device  for  Distributing  the  Wash-water  under 
the  Sand  Layer. — The  device  used  for  dis 
tributing  the  water  beneath  the  sand  layer 
comprised  the  outlet  pipe,  main  casting,  set 
of  parallel  pipes,  and  strainer  cups,  employed 
during  filtration  as  the  collecting  strainer  sys 
tem. 

As  this  device  has  already  been  described, 
it  will  not  be  repeated  here.  For  the  purpose 
of  breaking  the  nozzle  effect  of  the  neck  of 
the  strainer  cups,  a  small  casting  consisting 
of  a  ring  and  four  arms  connecting  at  the 
center  was  put  in  the  cup  when  it  was  made. 
(See  Plate  VTIT.)  The  total  area  of  the  necks 
of  the  strainer  cups  was  equal  to  a  4.1 2-inch 
pipe,  or  68  per  cent,  of  the  wash-water  supply 
pipe. 

Collecting  Clianncl. — The  space  between  the 
filter  tank  and  the  main  tank  was  used  as  a 
collecting  channel,  the  water  overflowing  the 
edge  of  the  inner  tank.  This  channel  was 
nominally  0.33  foot  wide,  but  owing  to  warp 
ing  and  other  displacements  of  the  inner 
tank  it  varied  from  0.2  to  0.4  foot.  A  suitable 
valve  controlled  the  flow  from  this  channel 
to  the  sewer  through  an  8-inch  pipe  about  9 
feet  long. 

Agitator. — The  agitating  device  consisted 
of  a  set  of  four  rake-arms  hung  from  a  vertical 


shaft  on  the  upper  end  of  which  was  a  hori 
zontal  gear  engaging  a  worm  on  a  horizontal 
shaft.  This  shaft  was  driven  by  a  small  en 
gine.  These  portions  of  the  agitator  are  next 
taken  up  and  described  in  detail. 

During  the  first  part  of  the  test  (up  to 
June  2)  a  double-thread  worm  was  used.  On 
this  date  a  single-thread  worm  was  installed. 
The  dimensions  of  this  worm  were:-  Outside 
length,  4  inches;  pitch,  I  inch;  smallest 
diameter,  2.75  inches;  and  largest  diameter, 
4  inches.  Both  worms  were  of  steel. 

The  dimensions  of  the  gear  were:  Outside 
diameter,  16.5  inches;  inside,  16.188  inches; 
and  pitch,  i  inch.  The  ratio  of  revolutions  of 
the  agitator  shaft  to  revolutions  of  the  main 
driving  shaft  was  i  :  49.  The  central  portion 
of  this  gear  was  of  iron,  and  the  teeth  were  of 
bronze  metal. 

The  vertical  shaft  which  carried  the  rake- 
arms  was  i  .8 1  inches  in  diameter.  The 
weight  of  the  shaft  and  rake-arms  was  sup 
ported  by  the  bearing  of  the  gear  above  men 
tioned,  the  whole  system  being  hung  from 
this  support.  At  the  lower  end  a  collar 
working  on  the  inlet  pipe  leading  from  the 
settling  chamber  served  as  a  guide. 

Attached  to  the  vertical  shaft  above  men 
tioned  was  a  casting,  in  which  there  were 
sockets  holding  the  rake-arms,  four  in  num 
ber.  The  casting  was  fastened  to  the  shaft 
by  two  set-screws,  and  it  was  also  sup 
ported  by  a  collar  1.75  inches  wide  fastened  to 
the  shaft  by  two  set-screws. 

The  arms  were  steel  rods  1.75  inches  in 
diameter.  They  were  fastened  into  the  sock 
ets  by  key  bolts.  There  were  two  long  and 
two  short  arms,  set  alternately  about  90° 
apart.  One  of  the  long  arms  was  4.67  feet 
long,  the  other  4.33  feet  long.  The  short 
arms  were  2.17  feet  and  1.58  feet  long,  re 
spectively.  The  longest  arm  had  seven  teeth, 
the  next  six  teeth,  and  each  of  the  short  arms 
three  short  teeth  and  chains.  On  the  long 
arms  the  teeth  averaged  3.69  feet  in  length  be 
low  the  center  of  the  arms.  Short  teeth  (2  feet 
long)  were  used  on  the  short  arms,  each  hav 
ing  22  inches  of  o.44-inch  chain  attached. 

The  teeth  were  made  of  iron  bars,  0.87  inch 
square  in  section,  set  so  that  one  diagonal  was 
tangent  to  the  arc  of  movement.  They  were 
attached  to  the  arms  by  wrist-joints  allowing 


DESCRIPTION   OF  FILTERS. 


8t 


them  to  turn  freely  in  a  left-hand  direction, 
but  holding  them  vertically  when  the  move 
ment  of  the  agitator  was  left-handed,  the  teeth 
turning  in  a  right-handed  direction  on  the 
arms.  By  this  device  the  teeth  were  made  to 
penetrate  the  sand  to  the  full  depth  at 
once. 

When  in  their  lowest  position  the  distance 
between  the  teeth  and  lowest  portion  of  the 
sand  was  about  0.25  foot. 

Engine.- — -The  engine  was  a  small,  double- 
cylinder,  reversible,  marine  engine,  with  both 
pistons  connected  directly  to  a  single  hori 
zontal  shaft  by  crank  arms  set  at  90°.  The 
main  dimensions  of  the  engine  were:  Cylin 
ders,  3  inches  in  diameter;  stroke,  4.125 
inches;  and  cut-off  at  85  per  cent.  On  the 
outer  end  of  the  shaft  there  was  a  fly-wheel 
2  feet  in  diameter,  having  an  approximate 
weight  of  90  pounds. 

The  driving  shaft  was  1.23  inches  in  diam 
eter.  From  the  center  of  the  engine  to  the 
center  of  the  worm  the  distance  was  5.625 
feet. 

Elevations. 

The  different  elevations  in  feet,  referred  to 
the  bottom  of  the  sand  layer  as  the  datum 
plane,  were  as  follows: 

Bottom  of  sand  layer  (top  of  strainer 

floor) o.oo 

Top  of  filter  tank  (wash-water  over 
flow)  +  3.41 

Sand  surface  (average  Aug.  i,  1896).  .   +2.54 

Crest  of  central  well +  3.68 

Center  of  rake-arms +  3.93 

Lower  end  of  rake-teeth  (during  wash 
ing)  +  0.24 

Average  maximum  water  level +  5.27 

Lower  floor  (main-house  floor) -  9.13 

Center  of  supply  pipe  at  settling  basin.  -  6.05 
Center  of  outlet,  wash  and  waste  pipes 

at  cross -  6.38 

THE  WESTERN  GRAVITY  FILTER  AND 
APPURTENANCES. 

Water  from  the  common  settling  chamber 
used  for  both  Western  Systems  passed 
through  this  filter  by  gravity.  The  sand  layer 


was  contained  in  a  vertical  wooden  tank,  and 
the.  open  compartment  in  the  tank  above  the 
sand  contained  the  water  to  be  filtered. 

During  filtration  the  water  passed  down 
ward  through  the  sand  and  was  collected  by 
a  manifold  of  slotted  brass  tubes  into  a  single 
outlet  pipe,  through  which  it  flowed  to  the 
sewer.  There  were  two  outlets  on  this  pipe, 
for  use  as  a  filtered-water  outlet  and  a  waste- 
water  outlet,  respectively,  as  the  operator 
deemed  advisable.  When  it  seemed  advisable 
to  wash  the  sand  the  supply  of  water  from  the 
settling  chamber  was  shut  off,  and  the  filter 
allowed  to  drain  more  or  less  completely.  The 
water  remaining  above  the  sand  was  drawn 
off  by  means  of  a  circumferential  gutter  at  the 
periphery,  an  outlet  from  which  connected 
with  the  sewer.  Wash-water  was  then  intro 
duced  into  the  wash-water  distributing  system 
and  forced  up  through  the  sand.  The  wash- 
water  after  passing  up  through  the  sand  over 
flowed  into  the  collecting  gutter,  from  which 
it  passed  into  the  sewer. 

The  total  available  acting  head  was  about 
14  feet. 

Before  entering  into  a  more  detailed  de 
scription  of  this  filter,  it  is  necessary  to  state 
that  under  the  name  of  the  Western  gravity 
filter  two  essentially  different  filters  were 
examined. 

The  original  filter  (operated  up  to  March 
22)  differed  from  the  final  filter  (put  in  ser 
vice  July  2)  in  the  following  points: 

1 .  Location  of  the  sand  layer,  the  final  filter 
having  its  sand  layer  7.0  feet  higher  than  the 
original  one. 

2.  Washing  device,  the  final  filter  having  a 
special  arrangement  for  distributing  the  wash- 
water,  while  in  the  original  filter  the  strainer 
manifold  for  the  collection  of  filtered  water 
alone  was  used. 

On  account  of  the  many  modifications  inci 
dental  to  the  changes  above  noted,  it  seems 
best  to  consider  two  filters,  Western  gravity 
filter  (A)  and  Western  gravity  filter  (B). 
What  has  already  been  said  applies  to  both 
niters.  All  elevations  used  are  in  feet  and  re 
fer  to  the  level  of  the  bottom  of  the  sand 
layer  of  the  Western  pressure  filter  as  the 
datum  plane.  The  drawings  (Plates  VI  and 
VII)  give  a  plan  and  section  of  Western 
gravity  filter  (B),  with  reference  lines  to  the 


82 


WATER  PURIFICATION  AT  LOUISVILLE. 


location  of  the  sand  layer  and  the  strainer 
floor  of  Western  gravity  filter  (A). 

Western  Gravity  Filter  (A). 

This  filter  was  placed  in  a  circular  wooden 
tank  which  was  open  at  the  top. 

About  one  foot  of  the  lower  portion  of  the 
tank  was  filled  with  a  layer  of  broken  stone, 
concrete,  and  cement,  by  which  the  sand 
layer  was  supported.  A  manifold  of  slotted 
brass  tubes  which  formed  the  strainer  sys 
tem  was  half  buried  in  the  cement.  The  inlet 
pipe  entered  the  tank  at  the  top  and  dis 
charged  into  a  circumferential  trough,  the 
crest  of  which  was  1.69  feet  above  the  sand 
and  8.24  feet  below  the  top  of  the  tank.  The 
upper  portion  of  the  tank  held  the  water  to  be 
filtered,  a  column  normally  about  8  feet  deep. 

Filter  Tank. — The  filter  tank  was  made  of 
pine  staves  2.75  inches  thick  and  4  inches 
wide.  It  was  smaller  at  the  top  than  at  the 
bottom,  being  m.o  feet  in  inside  diameter  at 
the  base  and  9.5  feet  in  inside  diameter  at  the 
top.  The  depth  was  14.37  feet-  It  was  bound 
strongly  by  ten  iron  bands,  each  0.25  inch 
thick,  and  ranging  from  3.5  inches  in  width 
at  the  bottom  to  2.5  inches  in  width  at  the 
top. 

/;//<•/  Water-pipe, — The  supply  pipe  to  the 
filter  connected  with  the  outlet  pipe  from  the 
settling  chamber,  and  passed  up  over  the  edge 
of  the  tank  and  down  on  the  inside,  discharg 
ing  into  the  circumferential  trough.  This 
pipe,  from  its  junction  with  the  outlet  from 
the  settling  chamber,  was  4  inches  in  diam 
eter.  From  the  settling  chamber  to  the  point 
where  this  pipe  began  there  were  about  10 
feet  of  6-inch  pipe.  The  total  length  of  pipe 
from  the  settling  chamber  to  the  discharge 
in  the  filter  tank  was  about  41  feet.  Flow 
through  this  pipe  was  regulated  by  a  hand- 
valve  and  by  a  plug  operated  by  a  float  on 
the  water  in  the  filter  tank. 

Arrangements  for  the  Exit  of  the  Filtered 
Jl'atcr. — After  passing  through  the  sand,  the 
water  passed  through  the  strainer  system, 
consisting  of  a  manifold  of  slotted  brass  tubes; 
a  rectangle  of  iron  pipes  into  which  these 
tubes  were  screwed,  and  which  served  as  col 
lecting  pipes;  and  an  outlet  pipe  connecting 
the  rectangle  with  a  branch  where  two  dis 


charge  pipes,  the  filtered-water  and  waste- 
water  pipe,  respectively,  connected  with  the 
sewer. 

Strainer  System. — The  strainer  system  was 
a  manifold  of  slotted  brass  tubes  screwed  into 
a  rectangle  5  by  7  feet  of  6-inch  wrought-iron 
pipe.  The  drawings  show  the  arrangement 
of  these  tubes  in  Western  gravity  filter  (13). 
They  were  arranged  in  almost  the  same  man 
ner  in  Western  gravity  filter  (A),  except  that 
short  lengths  of  tube  were  screwed  into  the 
outside  of  the  rectangle  also. 

The  tubes  were  1.5  inches  in  inside  diame 
ter  and  laid  in  a  bed  of  concrete,  the  surface 
of  the  concrete  being  just  above  the  center 
of  the  tubes.  The  slots  were  circumferential, 
five  rows  of  slots  in  each  section,  two  above 
the  cement  floor  and  three  below,  the  lower 
ones  of  course  being  covered  up  with  con 
crete.  They  were  cut  from  the  inside  by  a 
circular  saw  making  them  wider  and  longer 
on  the  inside  of  the  tube  than  on  the  outside. 
There  was  considerable  variation  in  the  length 
of  the  slots,  and  the  widths  differed  by  nearly 
50  per  cent.  An  average  of  several  deter 
minations  gave  a  length  of  0.719  inch  and  a 
width  of  0.024  inch.  The  slotted  sections 
were  spaced  0.125  inch  from  center  to  center. 
(See  Plate  VIII.) 

Exit  Area. — The  total  length  of  cut  tubing 
was  727  inches.  The  exit  area  per  linear  inch 
was  0.272  square  inch,  making  the  total  orifice 
area  198  square  inches. 

Outlet  Pi  fie. — The  outlet  was  a  4-inch  pipe 
connecting  with  the  strainer  manifold  in  the 
middle  of  one  of  the  short  sides  of  the 
rectangle.  From  this  point  it  led  out  through 
the  side  of  the  tank  and  to  the  front  of  the 
filter,  a  distance  of  about  8  feet,  where  it 
branched  into  a  filtered-water  and  a  filtered 
waste-water  pipe,  the  two  latter  pipes  con 
necting  with  the  sewer  6  feet  beyond. 

Sand  Layer. 

The  sand  layer  was  the  same  throughout 
the  use  of  this  filter.  Sand  No.  6,  a  natural 
sand,  was  used.  Mechanical  analysis  of  this 
sand  gave  results  which  are  presented  on  the 
next  page. 

Thickness  of  Sand  Layer. — The  nominal 
thickness  of  the  sand  layer  was  about  3  feet. 
The  thickness  as  determined  January  16  was 


DESCRIPTION  OF  FILTERS. 


MECHANICAL    ANALYSIS    OF    THE    SAND    USED 
IN    THE    WESTERN    GRAVITY    FILTKR(A). 

Number  6. 

I'crci-nl.  by  weight. 

100.00 

90. (» 

19.00 

...  3.60 

o  oo 


Finer  than  2.04     millimeters 

"     °-93  ^          

"     0.46  

"     0.316  "         

"0.182  "         

Effective  j  Ten   per   cent,  finer  than  /  n< 

size       (      diameter  in  millimeters  )"' 

36  inches  above  the  strainers.  On  March  20 
about  2  inches  were  scraped  off  the  surface 
after  the  close  of  the  day's  operations.  The 
sand  surface  was  level. 

Area. — The  area  of  the  sand  surface  was 
that  of  an  unbroken  circle  g  feet  10  inches  in 
diameter,  which  is  equal  to  75.94  square  feet. 

Device  for  Cleaning  the  Sand  Layer. 

The  device  for  cleaning  the  sand  comprised 
the  following  principal  parts,  which  are  de 
scribed  in  turn  below: 

1.  Pipes  through  which  the  filtered  water 
was  pumped  from  the  filtered-water  reservoir 
to  the  wash-water  distributing  pipes. 

2.  A    system   of   piping   to   distribute    the 
water  under  the  sand  and  thus  cause  its  dis 
tribution  through  the  sand  layer  during  its 
upward  passage. 

3.  A  collecting  gutter  and  pipes  to  carry 
to  the  sewer  the  water  remaining  above  the 
sand  after  draining,  and  the  wash-water  after 
passage  through  the  sand  during  washing. 

Wash-water  Supply  I'ipc. — The  wasli-wat  er, 
taken  from  the  filtered-water  reservoir,  was 
pumped  through  60  feet  of  8-inch  pipe  and  55 
feet  of  5-inch  pipe  to  a  point  of  connection 
with  the  outlet  pipe. 

Wash  -  water  Distrihnting  Pipes.  —  The 
strainer  system  of  slotted  brass  tubes  was 
used  as  a  wash-water  distributing  system. 

Collecting  Gutter. — A  circular  wooden  gut 
ter,  12  inches  deep  and  made  of  o.375-inch 
pine  boards,  was  fastened  to  the  inner  wall 
of  the  tank  0.6  foot  above  the  sand.  This  was 
used  to  carry  off  the  wash-water  after  passage 
through  the  sand,  and  a' pipe  at  the  front  with 
a  suitable  valve  connected  it  with  the  sewer. 

Elevations. 

The  different  elevations  in  feet,  referred  to 
the  bottom  of  the  sand  layer  of  the  Western 


pressure  filter  as  the  datum   plane,  were  as 
follows: 

Bottom  of  sand  layer  (top  of  strainer 

floor)    -    0.78 

Sand  level  (average  March  22,  1896).  +    2.22 

Crest  of  collecting  gutter +    3.91 

Top  of  tank +12.15 

Average  maximum  water  level +  1 1.90 

Lower  floor  (main-house  floor) -    2.22 

Center  of  outlet  pipe  at  filter -   0.95 

Western  Gravity  Filter  (B\ 

The  second  filter  operated  under  the  name 
of  the  Western  gravity  filter  differed  from 
the  first  one  in  the  location  of  the  sand  layer 
and  the  device  for  distributing  the  wash- 
water.  The  manner  of  operation  was  practi 
cally  the  same,  except  that  a  special  wash- 
water  distributing  device  was  used.  Connec 
tion  was  also  made  from  the  wash-water  pipe 
to  the  collecting  strainer  system,  whereby  the 
latter  could  be  used  to  distribute  wash-water 
if  desired,  and  also  in  order  to  loosen  the  sand 
around  the  strainers  by  forcing  water  through 
them.  The  normal  depth  of  water  above  the 
sand  during  filtration  was  3  feet. 

Filter  Tank. — The  tank  used  was  the  same 
as  that  used  by  the  Western  gravity  filter 
(A). 

Strainer  Floor. — The  strainer  floor  was  lo 
cated  8.37  feet  above  the  house  floor,  or  7 
feet  higher  than  in  the  first  filter.  This  was 
accomplished  by  building  a  second  flooring 
of  3-inch  pine  planks  supported  by  eight  4  by 
6-inch  pine  posts.  The  lower  part  of  the  tank 
was  not  used  with  this  filter,  but  was  kept 
filled  with  water  throughout  the  remainder 
of  the  test.  On  the  wooden  floor  was  laid  a 
layer  of  broken  stone  and  concrete  faced  with 
cement.  The  wash-water  system,  consisting  of 
distributing  pipes  and  ball  nozzles,  was  buried 
in  this  cement  layer.  The  top  of  the  cement 
was  flush  with  the  face  of  the  nozzles.  The 
strainer  system,  consisting  of  a  manifold  of 
slotted  brass  tubes,  was  laid  on  top  of  the 
cement  floor. 

The  relation  of  the  inlet,  outlet,  and  waste- 
water  pipes  to  the  sand  layer  was  the  same  as 
in  the  Western  gravity  filter  (A). 

Arrangements  for  the  Exit  of  the  Filtered 


WATER  PURIFICATION  AT  LOUISVILLE. 


Water. — After  passage  downward  through 
the  sand  the  water  flowed  into  the  strainer 
tubes,  a  manifold  of  which  covered  the  bot 
tom  of  the  filter  tanks.  From  this  manifold  a 
single  pipe  led  to  the  filtered-water  and  waste- 
water  outlets  as  in  Western  gravity  filter 
(A),  the  main  change  being  the  insertion  of  7 
more  feet  of  pipe  necessitated  by  the  increased 
elevation  of  the  sand  layer. 

Strainer  System. — The  strainer  system  was 
composed  of  slotted  brass  tubes  set  in  a 
rectangle  of  6-inch  wrought-iron  pipes.  It 
was  laid  on  top  of  the  cement  floor,  however, 
and  not  imbedded  in  it,  the  entire  slotted  area 
of  the  tubes  being  utilized.  Instead  of  con 
forming  to  the  sides  of  the  tank  as  in  Western 
Gravity  Filter  (A),  the  strainer  tubes  formed 
a  rectangle. 

The  strainer  tubes  were  nominally  spaced 
12  inches  from  center  to  center,  but,  as  will 
be  seen  from  the  drawing  (Plate  VI),  there 
were  several  places  on  the  floor  of  the  filter 
where  the  nearest  tubes  were  more  than  i  foot 
apart.  On  the  side  of  the  rectangle  at  the 
center,  the  distance  to  the  nearest  strainer 
slot  was  approximately  15  inches,  while  at  the 
corners  the  distance  was  about  18  inches.  In 
general  the  arrangement  covered  the  center 
of  the  bed  uniformly,  but  was  not  well  ar 
ranged  to  drain  the  sand  at  the  periphery. 

Exit  Aim. — The  total  length  of  strainer 
tubes  used  was  39.3  feet.  The  orifice  area  per 
linear  inch  was  0.680  square  inch,  making  the 
total  area  about  320  square  inches.  (For  de 
tails  of  the  strainer  system  see  Plate  VIII.) 

Sand  Layer. 

The  sand  layer  was  made  up  of  a  mixture 
of  sands  in  the  following  manner:  Approxi 
mately  12  inches  of  a  natural  sand  (No.  9) 
were  put  into  the  filter  and  washed  for  six 
minutes.  One  inch  of  fine  material  was  then 
scraped  off  the  top  and  discarded.  Sample 
No.  10  was  taken  after  this  sand  had  been 
washed  and  scraped.  The  sand  which  was 
used  in  Western  gravity  filter  (A),  (No.  7), 
was  then  screened  through  a  No.  24  sieve, 
and  all  of  that  which  would  pass  through  it 
(about  one-half)  was  discarded.  About  fwo 
feet  in  depth  of  the  screened  sand  were  then 
put  in  the  filter  and  the  coarse  and  fine  washed 


Finer  than  3.90    mm 

IOO.O    IOO.O    IOO.O    IOO.O    I 

'     2  .  04 

100.0     95.5  100.0     98.0  i 

0-93       ' 

95.5     66.  o    93.0     89.0 

0.46 

22.0      25/0       35.0       lg.0 

0.316    ' 

1.7       12.0         4.0         3.9 

0.182     ' 

o.o       i.o       o.i       o.g 

0.105     ' 

o.o      o.o      o.o      o.o 

("Ten   per  cent"! 

Effective!     finerthandi-l                                      g 
size       ]    ameter       in  [ 

[    millimeters   J 

together  for  ten  minutes.  Finally,  on  April 
30,  enough  more  of  the  screened  sand  was 
added  to  make  the  layer  three  feet  thick.  It 
was  then  thoroughly  washed  and  ready  for 
service.  Sample  No.  1 1  w«  from  the  final 
sand  when  ready  for  use.  Sample  No.  14  was 
collected  at  the  close  of  the  test,  Aug.  i,  1896. 
Mechanical  analyses  of  these  sands  gave  the 
following  results: 

MECHANICAL   ANALYSES   OF   THE   SANDS   USED 
IN    THE    WESTERN    GRAVITY    FILTER   (B). 

No.  7.    No.  9.    No.  10.  No.  ji.  No.  14. 
Per  cent,  by  weight. 


Thickness  of  Sand  Layer. — The  nominal 
thickness  was  36  inches.  On  July  25,  how 
ever,  the  thickness  was  found  to  be  only  31 
inches.  The  same  thickness  was  found  at  the 
close  of  the  test,  August  i. 

Area. — On  acount  of  the  sloping  sides  of 
the  filter  tank  the  area  was  less  than  in  West 
ern  gravity  filter  (A),  being  72.78  square 
feet. 

Device  for  Cleaning  the  Sand  Layer. 

The  device  for  cleaning  the  sand  consisted 
of  the  following  principal  parts,  which  are  de 
scribed  in  turn  below. 

1.  Pipes    through    which    the    wash-water 
was  supplied  to  the  wash-water  distributing 
system. 

2.  A  system  of  piping  and  ball  nozzles  used 
to  distribute  the  wash-water  under  the  sand 
layer. 

3.  A  secondary  system  for  the  distribution 
of  the  wash-water  under  the  sand  layer  (com 
prising  the  strainer  manifold). 

4.  A  collecting  gutter  and  pipes  to  carry 
to  the  sewer  the  last  portion  of  the  water  re 
maining  on  the  sand  after  draining  prepara 
tory  to  washing  the  filter,  and  also  to  carry 
off  the  wash-water  after  its  passage  through 
the  sand. 

Wash-water  Supplv  Pipes. — The  same  pip 
ing  was  used  as  in  the  Western  gravity  filter 


DESCRIPTION  OF  FILTERS. 


(A)  to  convey  the  filtered  water  to  the  con 
nection  with  the  wash-water  pipe  at  the  filter. 

During  the  test  of  this  filter,  however,  un- 
filtered  wash-water  was  used,  except  on  the 
last  day,  July  30. 

For  the  use  of  unfiltered  water  a  connec 
tion  was  made  from  the  main  inlet  pipe  to 
the  settling  chamber  with  the  wash-water 
pipe  at  the  meter,  the  filtered  wash-water  pipe 
being  disconnected. 

Beyond  the  meter  there  were  two  branches 
taken  from  the  main  wash-water  supply  pipe, 
one  of  which  was  connected  with  a  6-inch 
pipe  which  led  to  the  washing  device  in  the 
filter  tank,  a  distance  of  about  27  feet.  On 
this  pipe  was  located  a  swing  check  valve 
with  a  sand  pocket.  The  other  branch  from 
the  main  wash-water  supply  pipe  was  con 
nected  to  the  outlet  pipe  from  the  strainer 
system. 

When  filtered  water  was  used  the  main 
supply  pipe  was  disconnected,  and  in  its  place 
connection  was  made  with  the  filtered-water 
pipe  used  in  the  Western  gravity  filter  (A). 

Alain  Wash-water  Distributing  Device. — The 
main  wash-water  distributing  device  con 
sisted  of  a  manifold  of  pipes,  feeding  eighty- 
two  ball  nozzles  distributed  over  the  strainer 
floor  as  shown  in  the  drawing.  The  entire 
system  up  to  the  face  of  the  ball  nozzles  was 
covered  by  the  cement  floor. 

Sections  of  the  nozzles  are  shown  on  the 
drawings.  The  total  orifice  area  at  the  neck 
of  the  nozzles  was  made  up  of  eighty-two  0.5- 
inch  pipes  equaling  a  5.i88-inch  pipe.  All 
of  the  balls  were  of  solid  rubber,  and  had  a 
diameter  of  1.625  inches.  The  construction 
allowed  them  a  rise  and  fall  of  about  0.5  inch. 
With  the  ball  at  full  height  the  orifice  area 
was  approximately  1.4  square  inches  for  each 
nozzle.  The  inner  face  of  the  nozzle  was 
ground  to  allow  the  ball  to  make  a  close  fit 
and  so  shut  off  the  sand  and  water  during 
filtration. 

Secondary  Wash-ivater  Distributing  Svstcm. 
— A  connection  was  made  so  that  the  strainer 
tubes  could  be  used  as  wash-water  distribu 
ters,  but  the  main  washing  was  given  through 
the  ball  nozzles,  the  water  being  turned 
through  the  strainers  for  the  last  minute 
only. 

Collecting  Gutter. — This  was  the  same  as  was 


used  in  the  Western  gravity  filter  (A),  but 
it  was  located  6.33  feet  above  its  former 
position. 

Elevations. 

The  different  elevations  in  feet,  referred 
to  the  bottom  of  the  sand  layer  of  the  West 
ern  pressure  filter  as  the  datum  plane,  were 
as  follows: 

Bottom  of  sand  layer  (top  of  strainer 

floor) +    6. 1 9 

Sand  surface  (average  Aug.  i,  1896).  +    8.78 

Crest  of  collecting  gutter +  10.24 

Top  of  tank +12.15 

Lower  floor  (main-house  floor) -    2.22 

Center  of  inlet  pipe  (highest  point).  .  -f  12.35 

Center  of  outlet  pipe  at  filter +    6.32 

Center  of  outlet  (lowest  point) -    1.62 

Center  of  outlet  (discharge) -    1.62 

THE  WESTERN  PRESSURE  FILTER. 

This  was  a  portion  of  a  continuous  series 
of  pipes  and  compartments  through  which 
the  water  passed  in  the  process  of  purification. 
There  was  no  restriction  of  the  pressure  from 
the  beginning  to  the  end  (outlet)  of  the  en 
tire  system,  except  such  as  was  caused  by  the 
resistance  of  the  piping,  sand  layer,  and 
strainer  system. 

The  filtering  medium  was  placed  in  one- 
half  of  a  closed  steel  cylinder,  the  other  half 
of  which  was  used  as  a  settling  chamber.  A 
supply  pipe  for  this  filter  connected  with  the 
cylinder  at  the  top  by  a  flange  joint.  In  the 
lower  part  of  the  filter  chamber  was  a  layer 
of  broken  stones,  concrete  and  cement.  The 
strainer  system,  consisting  of  a  set  of  s'otted 
brass  tubes,  was  half  buried  in  this  concrete 
layer,  the  surface  of  which  formed  the  floor 
for  the  sand  layer. 

During  filtration  the  water  was  admitted 
under  a  pressure  of  from  45  to  65  pounds  into 
the  portion  of  the  chamber  above  the  sand 
layer.  After  Feb.  29,  1896,  the  pressure  was 
kept  quite  uniformly  between  60  and  65 
pounds.  The  outlet  from  the  strainer  system 
was  then  opened  and  the  difference  in  pres 
sure  caused  the  water  to  pass  downward 
through  the  sand  layer,  through  the  slots  in 
the  strainer  tubes  and  thence  through  the 
collecting  pipes  and  outlet  to  the  sewer.  The 


WATER  PURIFICATION  AT  LOUISVILLE. 


average  total  available  acting  head  was  about 
140  feet,  as  the  full  pressure  in  the  supply  pipe 
was  available,  and  the  filtered  water  was  dis 
charged  into  the  sewer. 

At  such  times  as  it  seemed  necessary  or 
advisable  to  wash  the  filter,  a  valve  on  the 
supply  pipe  from  the  settling  chamber  was 
closed.  At  the  same  time  a  valve  on  a^branch 
from  this  pipe  which  led  to  the  sewer  was 
opened.  Wash-water  was  then  let  into  the 
outlet  system  through  connections  between 
the  two  pipes,  forced  up  through  the  sand 
and  out  through  the  inlet  pipe  and  branch 
to  the  sewer. 

Filter  Chamber. — The  filter  chamber  was 
cylindrical  in  section  with  dome-shaped  ends. 
The  principal  inside  dimensions  were:  Length 
in  the  center,  11.15  feet:  length  on  the  sides, 
8.71  feet;  diameter,  8.00  feet.  The  inlet  pipe 
entered  the  top  of  the  chamber  at  the  center 
of  the  compartment.  In  the  lower  portion  of 
the  compartment  was  placed  a  layer  of  broken 
stones,  concrete  and  cement,  about  2.1  feet 
thick  in  the  center.  The  strainer  system,  con 
sisting  of  a  frame  of  iron  pipe  and  a  set  of 
slotted  brass  tubes,  was  half  buried  in  this 
layer.  ( )n  top  of  this  floor  was  the  sand  layer, 
and  the  upper  portion  of  the  compartment  for 
a  space  about  1.7  feet  high  contained  the 
water  to  be  filtered.  The  inlet  pipe  and  a 
branch  therefrom  was  used  as  an  outlet  for 
waste  water  during  washing. 

Inlet  Water-pipe. — The  inlet  pipe  was  6 
inches  in  diameter  and  conducted  the  water 
from  the  outlet  of  the  settling  chamber  over 
to  and  into  the  filter  chamber  at  the  top.  It 
was  about  29  feet  from  the  point  where  it  con 
nected  with  the  settling  chamber  to  the  con 
nection  with  the  filter  chamber.  Connection 
with  the  steel  shell  was  made  by  a  flange, 
riveted  to  the  shell.  The  pipe  screwed  into 
this  flange.  At  first  there  was  no  provision 
for  breaking  the  flow,  but  it  was  soon  found 
that  the  impact  of  the  water  caused  consid 
erable  disturbance  in  the  sand  surface,  and  a 
6-inch  nipple  4  inches  long  was  screwed  into 
the  flange  from  the  inside.  A  6-inch  tee  was 
screwed  on  the  nipple,  the  long  arm  of  the  tee 
running  parallel  with  the  sides  of  the  cham 
ber. 

Arrangements  for  the  Exit  of  the  Filtered 
Water. — After  passage  through  the  sand,  the 


water  was  collected  by  a  manifold  of  slotted 
brass  tubes  set  in  a  frame  of  iron  pipe  made 
in  the  form  of  a  letter  H,  9.0  feet  long  and 
3.5  feet  wide.  From  the  center  of  the  cross- 
piece  of  the  H  a  single  outlet  pipe  led  down 
through  the  shell  of  the  cylinder  and  out  in 
front,  where  it  rose  above  the  floor,  dividing 
into  two  outlets,  for  the  effluent  and  filtered 
waste  water,  respectively,  both  of  which  con 
nected  with  the  sewer. 

Strainer  System. — The  strainer  system  was 
made  of  a  manifold  of  slotted  brass  tubes 
screwed  into  two  lines  of  6-inch  pipe.  The 
arrangement  is  shown  on  the  drawings.  The 
tubes  were  1.5  inches  in  diameter.  They  were 
partially  imbedded  in  a  concrete  floor,  the  floor 
line  being  just  above  the  center  of  the  tubes. 
The  slots  were  circumferential,  five  slots  in 
each  section,  two  of  them  above  the  floor  and 
three  below.  The  lower  ones  were  of  course 
covered  up.  They  were  cut  from  the  inside  by 
a  circular  saw,  making  the  slot  wider  on  the 
inside  than  on  the  outside,  or,  in  other  words, 
wedge-shaped.  As  the  depth  of  cutting  varied 
considerably,  the  width  and  length  of  the  slots 
varied  by  quite  a  percentage.  An  average 
of  many  determinations  gave  a  width  of  0.024 
and  a  length  of  0.719  inch.  The  slotted 
sections  were  spaced  0.125  mch  from  center 
to  center. 

Exit  Area. — The  area  was  made  up  of  731 
linear  inches  of  strainer  tube,  containing,  per 
linear  inch,  16  slots  of  an  area  of  .017  square 
inch  each,  giving  a  total  orifice  area  of  199 
square  inches. 

Outlet  Pipe. — The  strainer  manifold  as 
above  described  connected  by  a  tee  in  the 
center  to  a  6-inch  downcomer,  which  went 
through  the  bottom  of  the  filter  and  con 
nected  with  a  pipe  which  passed  out  from 
under  the  filter,  and  branched  up  above  the 
floor.  The  upward  bend  was  made  by  a  tee, 
the  long  arm  of  which  was  horizontal.  To 
the  outer  end  of  the  long  arm  the  wash-water 
pipe  was  joined.  Just  above  the  floor  the  outlet 
pipe  entered  a  cross.  The  opposite  arm  of 
this  cross  connected  to  the  inlet  pipe.  The 
two  horizontal  arms  connected  to  the  outlet 
and  waste  pipes,  respectively.  These  two 
pipes  passed  directly  to  the  sewer.  From  the 
strainer  to  the  cross  the  distance  was  about 
9.5  feet. 


DESCRIPTION    OF  FILTERS. 


Outlet  and  Waste  Discharges. — From  the 
opposite  sides  of  the  cross  branched  the  out 
let  and  waste-water  pipes,  4  inches  in  diam 
eter.  They  both  led  directly  to  the  sewer,  a 
distance  of  about  4.5  feet. 

Sand  Layer. 

Kinds  of  Sand  Used. — The  character  of  the 
sand  was  changed  twice,  a  slight  amount  of 
coarser  material  being  added  the  first  time  and 
some  line  sand  the  second  time.  Up  to  April 
8,  the  layer  was  composed  of  sand  No.  6, 
a  natural  quartz  sand.  Sand  No.  8  was  the 
same  sand  after  use,  the  sample  having  been 
collected  from  the  sand  which  was  removed 
April  8.  The  new  sand  layer  put  in  service 
May  8  was  made  up  in  the  following  manner: 

Approximately  12  inches  in  depth  of  sand 
No.  9,  a  natural  sand,  were  put  into  the  filter 
and  well  washed.  All  of  the  old  sand  was 
then  put  back,  and  on  top  of  this  12  inches 
of  the  original  sand  (No.  6)  were  added.  The 
sand  layer  was  then  washed  for  10  minutes 
under  unusually  high  pressure,  enough  sand 
being  washed  out,  it  was  estimated,  to  lower 
the  level  from  3  to  4  inches.  On  June  3  about 
6  inches  of  the  original  sand  (No.  6)  were 
added.  Sample  No.  15  was  taken  of  the  sand 
in  use  at  the  close  of  the  test.  Mechanical 
analyses  of  these  sands  gave  the  following 
results: 

MECHANICAL    ANALYSES    OF  THE  SANDS    USED 
IN  THE  WESTERN   PRESSURE  FILTER. 


No. 

6. 

No. 

No.  9. 

No. 

15. 

Perc 

•  : 

by  wei(,'h 

t. 

nerthan 

3.90  i 

nillimeters 

IOO 

O 

IOO 

O 

IOO.O 

ii  •') 

0 

2.04 

1 

IOO 

O 

IOO 

O 

95-5 

IOO 

0 

" 

0-93 

96 

o 

93 

o 

66.0 

95 

.5 

'  ' 

0.46 

' 

"9 

o 

14 

5 

25.0 

15 

I 

0.316 

3 

.6 

i 

o 

12.  0 

O 

•4 

0.182 

0 

.0 

o 

I 

I  .O 

o 

.0 

0.105 

o 

o 

o 

o 

o.o 

o 

.0 

fective  I 
size      j 

Ten  percent  finer  ] 
than  diameter  in   [      o 
millimeters.       ) 

•39 

o 

43 

0.30 

o 

•44 

Thickness  of  Sand  Layer. — The  thickness 
of  the  sand  layer  was  changed  twice  intention 
ally.  On  Jan.  13  it  was  4.00  feet  deep.  Prac 
tically  no  change  took  place  from  that  date 
until  April  8,  when  the  sand  was  removed. 
The  new  layer  put  in  service  May  8  was  esti 
mated  to  be  4.85  feet  thick  before  it  was 
washed.  On  June  3  the  thickness  was  found 
to  be  4.27  feet  or  7  inches  less,  of  which  it  was 
estimated  that  4  inches  was  caused  by  settling 


and  3  inches  by  removal  in  washing.  On  this 
date  ten  sacks  of  sand  (No.  6)  were  added. 
The  thickness  as  determined  July  15  was  4.71 
feet.  After  the  close  of  the  test,  Aug.  i, 
1896,  it  was  found  to  be  4.12  feet. 

Sand  Surface. — The  major  portion  of  the 
sand  surface  was  level.  In  the  center  the  im 
pact  of  the  water  from  the  inlet  formed  a  de 
pression,  about  3  feet  in  diameter  and  3  inches 
to  4  inches  deep.  The  introduction  of  a  tee  on 
the  inlet  pipe  remedied  this  trouble. 

Area. — The  determination  of  the  available 
filtration  area  of  the  sand  layer  was  compli 
cated  by  the  following  facts: 

The  sides  and  ends  of  the  layer  were  curves, 
and  every  change  in  thickness  changed  the 
area  of  the  layer. 

The  sand  surface  did  not  form  a  sharp 
junction  with  the  side  wall,  but  for  a  depth, 
apparently,  of  from  i  to  2  inches  the  sand 
curved  away  from  the  wall. 

As  the  sides  and  ends  of  the  sand  layer  were 
curved,  the  upper  surface  was  less  in  area  than 
a  section  at  the  center  of  the  chamber. 

Inasmuch  as  it  is  the  surface  of  the  sand 
which  removes  the  major  portion  of  the  sedi 
ment,  and  as  it  is  customary  in  this  connec 
tion  to  use  the  surface  of  the  sand  as  a  basis 
of  computation,  it  is  deemed  advisable  to  use 
this  as  the  filtration  area.  Further,  as  the 
thickness  varied  considerably  during  the  test 
it  was  thought  advisable  to  take  the  area  as 
first  measured  and  use  it  in  current  work,  cor 
recting  at  the  close  if  necessary.  The  area 
used  was  determined  from  measurements 
taken  Jan.  13,  which  were  as  follows:  Length 
at  the  side,  9.07  feet;  length  at  the  center. 
10.35  feet-  an(l  width,  6.67  feet.  The  laps 
at  the  ends  somewhat  reduced  the  area,  the 
surface  as  determined  being  66.22  square  feet. 
Redetermination  after  the  close  of  the  test 
gave  an  area  of  65.30  square  feet,  the  change 
being  due  to  the  increased  depth  caused  by 
adding  more  sand.  This  area  was  determined 
from  the  following  measurements: 
Approximate  radius  of  ends  of  sur 
face  8.92  feet. 

Middle  ordinate  of  curve 0.60    '' 

Length  of  rectangular  portion  of 

surface 9.03    ' 

Total  length  of  surface  at  center.  .    10.23    ' 
Width  of  surface  at  center 6.67    " 


WATER   PURIFICATION  AT  LOUISVILLE. 


For  the  purpose  of  comparison  the  follow 
ing  areas  are  presented: 

Area  of  sand  surface  (Jan. 

13,  1896) 66.2  square  feet. 

Area  of  sand  surface  (Aug. 
i,  1896) 65.3 

Area  of  surface  of  strainer 
floor 72.8 

Area  of  maximum  hori 
zontal  section  of  filter 
chamber 83.3 

The  difference  between  the  areas  as  deter 
mined  Jan.  13  and  Aug.  i,  1896,  is  only  1.4 
per  cent.,  and  inasmuch  as  the  related  obser 
vations  were  liable  to  a  greater  percentage 
error,  it  has  been  thought  best  to  use  the  orig 
inal  area  of  66.22  square  feet  in  all  computa 
tions.  On  May  8  the  area  was  probably  10 
per  cent,  less  than  this,  but  it  increased 
rapidly  for  three  or  four  days,  owing  to  loss  of 
sand  during  washing,  and  was  probably  not 
over  2  or  3  per  cent,  less  than  this  during 
the  balance  of  the  test. 

Device  for  Cleaning  the  Sand  Layer. 

The  device  used  for  cleaning  the  sand 
layer  by  washing  comprised  the  following 
parts: 

1 .  Pipes  through  which  the  wash-water  was 
conveyed  to  a  connection  with  the  distribut 
ing  pipes. 

2.  Pipes  for  the  distribution  of  the  wash- 
water  under  the  sand  layer  during  washing. 

3.  An  exit  pipe  for  the  wash-water  after  it 
had  passed  through  the  sand. 

Wash-ivater  Supply  Pipe. — During  the 
major  portion  of  the  test  filtered  water  was 
used  as  wash-water.  From  June  4  to  July  27, 
inclusive,  unfiltered  water  was  used. 


The  supply  of  filtered  water  was  pumped 
from  the  filtered-water  reservoir,  through 
the  same  pipes  as  supplied  the  gravity  filter, 
to  the  wash-water  meter,  a  distance  of  115 
feet.  From  this  point  a  separate  6-inch  pipe 
led  to  a  connection  with  the  outlet  pipe  of 
the  pressure  filter,  a  distance  of  about  18 
feet.  ' 

For  the  use  of  unfiltered  wash-water  the 
connection  with  the.  filtered-water  supply  pipe 
at  the  meter  was  disconnected  and  replaced  by 
a  connection  with  the  main  river-water  pipe 
leading  to  the  settling  chamber. 

Pipes  for  the  Distribution  of  IV ash-water. — 
The  outlet  pipe  conveyed  the  wash-water  to 
the  strainer  tubes,  which  were  used  to  dis 
tribute  the  water  under  the  sand  layer  during 
washing. 

Exit  Pipe  for  Wash-water. — The  inlet  or 
supply  pipe  was  used  as  an  exit  pipe  for  the 
wash-water  after  its  upward  passage  through 
the  sand.  About  8  feet  from  the  connection 
of  this  pipe  with  the  shell  of  the  cylinder  a 
6-inch  pipe  branched  over  to  the  sewer,  a  dis 
tance  of  about  10  feet.  Suitable  valves  were 
provided  on  these  pipes  to  allow  their  use  as 
desired. 

Elevations. 

The  different  elevations  in  feet,  referred  to 
the  bottom  of  the  sand  layer  as  the  datum 
plane,  were  as  follows: 

Bottom    of    sand    layer    (surface    of 

strainer  floor) o.oo 

Surface  of  sand  layer  (Aug.  i,  1896).  .  +4.12 

Inner  side  of  cylinder  at  top +  5.84 

Center  of  discharge  tee  on  inlet  pipe .  .  +  5.25 

Lower  floor  (main-house  floor) -  2.22 

Center  of  outlet  discharge  at  sewer.  .  .  -  1.22 


SUMMARY  OF   THE    VARIOUS  PARTS   OF    THE  SYSTEMS. 


89 


CHAPTER  VI. 

SUMMARY  OF  THE  VARIOUS  PARTS  OF  THE    RESPECTIVE  SYSTEMS,   AND   A  RECORD   OF 
REPAIRS,  CHANGES   AND   DELAYS. 


IT  is  stated  in  the  introduction  to  this  re 
port  that  each  of  the  systems  described  in  the 
foregoing  chapters  represents  the  same 
method  of  purification,  and  that  they  differed 
only  to  a  certain  degree  in  the  various  devices 
employed  to  put  into  practical  use  the  same 
fundamental  principles.  In  this  chapter  it  is 
the  purpose  to  present  a  list  of  all  the  parts 
comprised  in  each  of  the  divisions  of  the  re 
spective  systems  employed  in  carrying  out 
this  method  of  purification,  which  consists  of 
three  steps,  viz.: 

1.  Application   of   chemicals   to    the   river 
water. 

2.  Coagulation  and  sedimentation. 

3.  Filtration. 

The  schedules  on  the  following  pages 
(Tables  Nos.  i,  2,  and  3)  show  the  various 
parts  comprising  a  system  which  in  each  case 
was  installed  to  purify  250,000  gallons  of  river 
water  per  24  hours,  according  to  the  contracts 
with  the  Water  Company.  They  are  of  value 
not  only  as  a  matter  of  record,  but  also  as  an 
indication  of  the  attention  necessary  for  their 
satisfactory  operation  and  maintenance.  It 
will  be  understood  that  these  schedules  refer 
only  to  the  systems  and  their  immediate  con 
nections. 

In  accordance  with  the  contracts  between 
the  several  Filter  Companies  and  the  Water 
Company  the  latter  provided  the  following 
portions  of  the  experimental  plant,  in  addi 
tion  to  the  laboratory: 

1.  The  houses  in  which  the  systems  were 
installed,  and  the  necessary  foundations  on 
which  they  rested. 

2.  All  water  and  steam  used  by  the  systems 
in  their  operation. 


3.  All  steam  and  water  pipes  leading  to  and 
from  each  system. 

4.  All  meters  for  the  measurement  of  the 
water. 

5.  A  reservoir  of  142,000  gallons  capacity 
for  storage  of  the  filtered  water  for  washing 
the  filters. 

6.  A  pumping  engine  of  3,000,000  gallons 
capacity  per  24  hours  to  deliver  filtered  water 
under  pressure  to  the  large  filters  for  wash 
ing^ 

The  general  location  of  the  chief  portions 
of  the  experimental  plant,  including  the  stor 
age  reservoir  and  wash-water  pump,  is  shown 
on  Plate  I. 

In  Tables  Nos.  i,  2,  and  3  are  given  lists  of 
the  principal  devices  employed  in  the  respec 
tive  systems  for  carrying  on  the  three  steps 
of  (his  method  of  purification. 

Table  No.  I  includes  all  the  principal  de 
vices  used  in  connection  with  the  application 
of  the  chemicals  to  the  river  water. 

Table  No.  2  contains  a  list  of  the  prin 
cipal  appurtenances  of  the  settling  cham 
bers. 

Table  No.  3  is  a  tabulation  of  the  principal 
devices  and  appurtenances  of  the  filters. 

In  the  tabulations  under  this  head,  only  the 
leading  dimensions  of  the  various  devices  are 
given,  and  reference  is  made  in  all  cases  to 
Chapters  IT,  IV,  and  V,  where  descriptions 
will  be  found,  and  to  the  drawings  on  which 
these  devices  are  shown.  All  devices  which 
were  in  design  or  construction  peculiar  to  the 
respective  system  in  which  they  were  used 
are  marked  with  a  star  (*).  All  other  devices 
are  understood  to  be  such  as  are  in  common 


9o 


WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE   No.   1. 

DEVICES    FOR    THE   APPLICATION   OF  THE   CHEMICALS   TO   THE    RIVER    WATER    BY   THE 

RESPECTIVE   SYSTEMS. 


Warren. 

Jewell. 

Western-Device  No.  i.                  Western-Device  No.  2. 

Mixing 
Tanks. 

Pump 
Boxes. 

Propeller 

Wheels. 

Pumps. 

Air 
Chambers. 

Air 
Compressors. 

Gauges. 

Glass  Sight 
Tubes. 

Platform 
Scales. 
Steel  Rods. 

Two    circular     white-pine 
tanks,  4  feet  in  diameter, 
4.5  feet  deep. 

One    rectangular    wooden 
box,  2.9  by  1.2  feet,  by 
i.o  feet  deep. 
One    seven-bladed    screw- 
wheel  made  of  cast  brass, 
diameter  0.5  foot,  depth 
0.2  foot.* 
One          vulcanized-rubber 
pump.* 

Two  circular  cypress  tanks 
3.5  feet  in  diameter,  5.5 
feet  deep. 
One  ordinary  "  half-bar 
rel"  of  oak,  iron-bound. 

One  vertical  iron  cylinder,  Two     circular    white-pine 
i  foot  in  diameter,  2  feet       tanks,  3  feet  in  diameter, 
deep.*                                   1     4  feet  deep. 

Two    single-acting   steam- 
pumps.     Size,  3.5  by  4.5 
by  6.0  inches. 

One  Worthington  pumping 
engine.      Size    8.5    by  9 
by  10  inches. 
Two     auxiliary     pumps; 
plunger  extensions  of  the 
piston-rods  of  the  main 
pump. 
One  cast-brass  cylinder,   3 
inches     in    diameter,     6 
inches  long. 
One    cast-iron   cylinder,  6 
inches  in  diameter,  2  feet 
long- 
One  wrought-iron  cylinder, 
5   inches  in   diameter,   4 
feet  long,  with  fittings. 
Two  wooden  depth  gauges. 

One   o.  5-inch    glass    sight 
tube,  1.5   feet  long  with 
brass  fittings. 
One    24O-pound    platform 
scale. 

Two    glass     sight    gauges, 
i.o    inch    in   diameter,  4 
feet  long,  with  brass  fit 
tings. 

Two  wooden  depth  gauges. 

One   o.  75-inch   glass  sight 
tube,  i.o  foot  long,  with 
brass  fittings. 
One    24O-pound    platform 
scale. 

One      celluloid       mercury 
sight  gauge  with  fittings; 
diameter    approximately 
0.25  inch. 

One    24o-pound     platform 
scale. 
6  feet  o.  5-inch  steel  rod. 

One    24O-pound     platform 
scale. 

Brass  Pipes. 

Brass 

Fittings. 

Brass 

Valves. 

Iron  Pipes. 
Iron  Fittings. 

Iron  Valves. 

Lead  Pipes. 
Rubber 
Valves. 

gears.* 
Two     4  inch     steel     bevel 
gears.* 
12  feet  i.  5-inch  brass  pipe. 

Twelve       i.5-inch        brass 
fittings. 

Two  i.  5-inch  brass  plugs. 
24  feet  i.  5-inch  iron  pipe. 

10  feet  o.  5-inch  brass  pipe. 
Five  o.  5-inch  brass  fittings. 

Two      o.  75-inch      brass 
valves. 
Three      o.  5-inch      brass 
valves. 
One    o.5-inch   brass   check 
valve. 
95  feet  o.  75-inch  iron  pipe. 
30  feet  o.  5-inch  iron  pipe. 
10  feet  i.o-inch   iron  pipe. 

10  feet  0.5  inch  brass  pipe. 

Eight    o.  5-inch    brass     fit 
tings. 

Twooo-inch  brass  valves. 

10     feet     o.75-inch     brass 
pipe. 
6  feet  0.5  -inch  brass  pipe. 
Nine    o.75-inch     brass  fit 
tings. 
Twenty-two  o.  5-inch  brass 
fittings. 
Twoo.  75-inch  brass  valves. 
Two       cast-brass        valve 
chambers  with  valves. 
Six  o.  5-inch  brass  valves. 
One  o.5-inch   brass   check 
valve. 
20  feet  o.75-inch  iron  pipe. 
12  feet  o.  5-inch  iron  pipe. 

Twelve   o.  75-inch  iron  fit 
tings. 
Eight  o.  5-inch  iron  fittings. 

Four  o.75-inch  iron  valves. 
Two  o.  5-inch  iron  valves. 
One    o.5-inch     iron    check 
valve. 

Two  i.  5-inch  iron  valves. 

7  feet  i.  5-inch  lead  pipe. 
Dne    i.  5-inch   rubber   float 
valve. 

Fifteen  o.  75-inch   iron    fit 
tings. 
Twenty   o.  5-inch    iron    fit 
tings. 
Five  o.  75-inch  iron  valves. 
Two  o.  5-inch  iron  valves. 
Three  i.o-inch  iron  valves. 
One    i.o  inch    iron     steam 
regulating  valve. 
25  feet  o.  75-inch  lead  pipe. 

SUMMARY  OF   THE    VARIOUS  PARTS  OF    THE   SYSTEMS. 


91 


TABLE    No.    2. 

DEVICES   FOR   THE   COAGULATION    AND   SEDIMENTATION   OF   THE    RIVER    WATER    BY    THE 

RESPECTIVE   SYSTEMS. 


Warren. 

Jewell. 

Western—  Device  No.  i. 

Western—  Device  No.  j. 

Settling 

One      open       rectangular 

The    lower    portion    of    a 

The      settling       chamber 

Same  as  device  No.  I. 

Basins  or 

wooden   basin,  12.1  feet 

circular    wooden     tank, 

formed    one    half    of    a 

Chambers. 

by    12.  o  feet,    by    10.25 

13.5    feet    in    diameter, 

steel       cylinder,       with 

feet  deep. 

14.0  feet  high. 

dome-shaped    ends,    S.o; 

Main    dimensions    of   set 

feet    in    diameter,    22.5 

tling   chamber  :     Diam 

long. 

eter,    13.0  feet  ;   depth, 

Inside    dimensions  of  the 

6.89  feet. 

settling        chamber  : 

Length   in  center,  11.15 

feet;  length  on  the  side, 

8.71   feet  ;  diameter,  8.0 

feet. 

Iron  Rod. 

48    feet     o.375-inch     iron 

rod. 

Iron 

2  feet  6-inch  iron  pipe. 

One      quarter      bend      of 

30  feet  S-inch  iron  pipe. 

24  feet  6-inch  iron  pipe. 

Pipes. 

halved  4-inch  iron  pipe. 

23  feet  4-inch  iron  pipe. 

Two      feet      8-inch      iron 

pipe. 

3  feet  4-inch  iron  pipe. 

0.5  foot  5-inch  iron  pipe. 

Iron 

Four  6-inch  iron  fittings. 

Two  8-inch  iron  fittings. 

Six  6-inch  iron  fittings. 

Seven  6-inch  iron   fittings. 

Fittings. 

Three  4-inch  iron   fittings. 

Two  5-inch  iron  fittings. 

Six  4-inch  iron  fittings. 

Six  4-inch  iron  fittings. 

Iron 

One   5-inch   balanced   iron 

One  8-inch  iron  valve. 

One  6-inch  iron  valve. 

One  6-inch  iron  valve. 

Body 

valve  operated  by  float. 

One    5-inch    single  seated 

One  4-inch  iron  valve. 

Valves 

One  4  inch  Map  valve 

valve  operated  by  float. 

One  5  inch  iron  valve. 

TABLE  No.   3. 

DEVICES    FOR    THE    FILTRATION    OF   THE   COAGULATED    AND    PARTIALLY    SUBSIDED    WATER  BY 

THE    RESPECTIVE   SYSTEMS. 


Warren. 

Jewell. 

Western  Gravity 

(A). 

Western  Gravity 
(B). 

Western  Pressure. 

Filter  Tanks. 

One  open  circular  wooden 

One  open  circular  wooden 

One  open  circu-  Same     as      listed 

One   half    of    the 

tank  ;   10.6  feet  in  diam 

tank,  12.15  feet  in  diam 

lar    wooden      under  Western 

steel      cylinder 

eter,  9.75  feet  deep. 

eter,  5.0  feet  deep. 

tank,   9.5   feet      gravity  (A). 

listed  under  set- 

in  diameter  at 

tlingchambers. 

the    top,    10.0 

Size    of    fi  1  1  er 

feet    in    diam 

compartment  : 

eter  at  the  bot 

Length  in  cen 

tom,  14.37  feet 

ter,  11.15  feet; 

deep. 

length  on  sides, 

8.71    feet;    di 

ameter,     8.00 

feet. 

Sand  Layers. 

Area,    77.36    square    feet  ; 
thickness,  2.25  feet  ;  vol 

Area,    115.8    square    feet; 
thickness,  2.54  feet;  vol 

Area,      75.94 
square      feet  ; 

Area,          72.78 
square       feet  ; 

Area,          85.30 
square     feet; 

ume,  6.5  cubic  yards. 

ume,  10.9  cubic  yards. 

thickness,    3.0      thickness,  2.58 

thickness,   4.12 

r 

88.25    square    feet    copper 

feet;    volume,  i     feet;    volume, 

feet  ;     volume, 

plate,    0.031    inch    thick, 

8.4        cubic 

7.ocubicyards. 

12.  o       cubic 

punched  with  0.043  inch 

yards. 

yards. 

holes,  78.6  to  the  square 

inch.* 

Strainer 
Systems. 

6  1.  9  square  feet  brass  gauze, 
65   meshes  to    the    linear 
inch. 

Seven     iron     castings     for 
strainer      manifold.* 
444  strainer  cups.* 

39.5     feet      1.5- 
inch       slotted 
brass  pipe.* 

38.0      feet       1.5- 
inch    slotted 
brass  pipe.* 

61    feet     i.  5-inch 
slotted       brass 
pipe.* 

15.5  square  feetbrassgauze, 

80  meshes  to   the   linear 

inch. 

172.5  feet  copper  strips  1.12 

inches  wide. 

Belts. 

60  feet  6-inch  rubber  belt. 

WATER  PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  3.  —  Continued. 


Warren. 

Jewell. 

Western  Gravity 
(A). 

Western  Gravity 
(B). 

Western  Pressure. 

Engines. 

)ne  vertical  single-cylinder 

3ne    double-cylinder      re 

engine. 

versible  marine  engine. 

Diameter  of  cylinder,   5.75 

Diameter    of   cylinder,    3.0 

inches  ;      stroke,      6.0 

inches  ;      stroke,      4.125 

inches. 

inches. 

Gears. 

Dne  35-inch  iron  gear.* 

3ne     steel     worm,     single 

One  26-inch  iron  gear.* 

thread  :  length,  4  inches; 

One    16.  5-inch    iron    bevel 

pitch,    I    inch  ;    smallest 

gear. 

diameter,     2.75     inches  ; 

Two  8.25-inch  iron  gears.* 

largest        diameter,        4 

One  6.25-inch  iron  gear.* 

inches.* 

One     6.o-inch     iron     bevel 

One  gear  made  of  iron  and 

gear.* 

bronze      metal  :     outside 

One  5.75-inch  iron  gear.* 

diameter,       16.5  inches  ; 

One  4.25-inch  iron  gear.* 

pitch,  i  inch.* 

One     3.o-inch     iron    bevel 

gear.* 

Pipes. 

One  length  8-inch  iron  pipe, 

8  feet  4-inch  iron  pipe. 

27     feet     4-inch 

48    feet    i.  5-inch 

3  feet  4-inch  iron 

4  feet  long.* 

2  feet  5-inch  iron  pipe. 

iron  pipe. 

iron  pipe. 

pipe. 

One  length  8-inch  iron  pipe, 

.8  feet  8-inch  iron  pipe. 

28     feet     6-inch 

25     feet      4-inch 

62      feet      6-inch 

3.75  feet  long.* 

iron  pipe. 

iron  pipe. 

pipe. 

One      iron      central     well  : 

2  feet  8  inch  iron 

60     feet      6-inch 

height,  4.33  feet  ;   diam 

pipe. 

iron  pipe. 

eter,  2.42  and  1.71  feet.* 

g  feet  8-inch  iron 

One  length  8-inch  iron  pipe. 

Pipe- 

6.75  feet  long.* 

4  feet  2-inch  brass  pipe. 

2  feet  3-inch  iron  pipe. 

12  feet  3-inch  iron  pipe.* 

CUnftc 

4  feet  4-inch  iron  pipe. 

shaft 

onaiis. 

i.o     feet      2.  5-inch      steel 
shaft. 

17.2    feet    i.  75-inch     stee 

1.81     feet     1.  25-inch      steel 

shaft. 

shaft. 

8  feet  i.  25-inch  steel  shaft. 

2.21    feet     1.  75-inch      steel 

shaft. 

3.87    feet     2.25-inch     steel 

shaft. 

I  pvf>r<5 

Two  sets  shifting  levers.* 

Rakes. 

Two  rake  arms.* 

One   iron   casting   for   sup 

Two  stiffener  arms.* 

port  of  rake-shafts.* 

Two    tie-rods   0.75   inch   in 

Thirteen      wrought-iron 

diameter,  5.5  feet  long. 

teeth,  3.69  feet  long,  0.87 

Sixteen  rake-teeth,  35  inches 

inch  square. 

long.* 

Six  wrought-iron  teeth,  2.00 

feet      long,      0.87      inch 

square. 

Pulleys 

One  20  inch     ulle 

it  feet  o.  44-inch  iron  chain. 

One  i8-inch  pulley. 

One  friction  clutch  for   18- 

inch  pulley. 

One  i6-inch  pulley. 

One  12-inch  pulley. 

ma'n 

Special 
Castings  for 

vertical  shaft,    25   inches 

gear  and  shaft. 

Agicator. 

long,     0.75     inch    thick 

Two    cast-iron    shaft    sup 

cast  with  a  helical  thread 

ports. 

three  threads  to  the  inch.* 

Framework     for      agitator 

machinery,  with  bearing 

plates. 

Fittings. 

Five  8  inch  iron  fittings. 

Three  8-inch  iron  fittings. 

Six    6-inch    iron 

Two   8-inch   iron 

Twenty-five       6- 

Seven  4-inch  iron  fittings. 

Four  5-inch  iron  fittings. 

fittings. 

fittings. 

inch     iron    fit 

Twelve  3-inch  iron  fittings 

Eighteen    4-inch    iron     fit 

Nine  4-inch  iron 

Six    6-inch     iron 

tings. 

Four  2-inch  brass  fittings. 

tings. 

fittings. 

fittings. 

Four  4-inch    iron 

Sixteen  2-inch  iron  fittings 

Five  4-inch   iron 

fittings. 

One  8  by  6  by  3-inch  tee.* 

fittings. 

Twelve    i.  5-inch 

iron  fittings. 

SUMMARY  OF   THE    VARIOUS  PARTS  OF   THE  SYSTEMS.  93 

TAHLE  No.  3. — Concluded. 


Warren. 

Jewell. 

Western  Gravity 

(A). 

Western  Gravity 
(B). 

Western  Pressure. 

Brass  and 

One   2-inch  brass  valve. 

One  8-inch  iron  valve. 

One  8-inch  iron 

One    8-inch    iron 

Five   6-inch    iron 

Iron  Body 

Two  8-inch  iron  valves. 

Three  5-inch  iron  valves. 

valve. 

valve. 

valves. 

Valves. 

One  6-inch  iron  valve. 

Two  4-inch  iron  valves. 

Four  4-inch  iron 

Two   6-inch    iron 

Two  4-inch    iron 

One  4-inch  iron  valve. 

valves. 

valves. 

valves. 

One  3-inch  iron  valve. 

Four  4-inch  iron 

valves. 

One  4-inch  brass 

plug  with  float 

and  float  arm. 

Special 

One   open    rectangular 

One  controller. 

Outlet 

wooden  box,  5.71  feet  by 

Regulating 

2.75  feet,  by    10.25  feet 

Devices. 

deep. 

One    iron    plate,   2.25    feet 

wide,  4.5  feet  long. 

One  worm  shaft  and  wheel 

with  stand. 

Broken  Stone, 

2  .  2    cubic   yards  brick  and 

2    n   rnhir    varHc 

,  .             . 

. 

Brick  and 

cement. 

broken     stone 

broken       stone 

3.0    cubic    yards 
broken   stone 

Cement. 

and  concrete. 

and  concrete. 

and  concrete. 

Special 

30  feet  i-inch  slotted  brass 

Devices  for 

pipe.* 

nozzles  ;    brass 

Distributing 

4.5  feet  2-inch  slotted  brass 

castings      with 

Wash-water.  I     pipe.* 

rubber  balls.* 

RECORDS  OF  THE  REPAIRS  AND  CHANGES  OF 
THE  VARIOUS  DEVICES  OF  THE  RESPEC 
TIVE  SYSTEMS. 

The  next  two  topics  of  this  chapter,  dealing 
respectively  with  the  repairs  and  changes 
which  were  made  during  these  investigations, 
are  closely  allied  to  each  other.  The  majority 
of  repairs  were  coincident  with  changes  of 
more  or  less  importance.  As  a  matter  of  con 
venience  for  reference  the  repairs  and  changes 
are  listed  separately,  so  far  as  it  is  practicable 
to  do  so,  on  the  basis  that  repairs  related  to 
work  done  on  devices  which  had  temporarily 
failed  to  serve  their  purpose,  and  that  changes 
refer  to  the  installment  of  new  devices  or  por 
tions  thereof  where  the  old  devices  did  not 
give  results  satisfactory  to  the  operators.  The 
repairs  and  changes,  with  the  total  periods 
occupied,  are  listed  in  the  next  two  tables. 
The  periods  refer  to  10  working  hours  per  day 
from  the  time  that  regular  operations  ceased 
until  they  began  again.  Whenever  possible 
repairs  and  changes  were  made  outside  of  the 
regular  hours  of  operation  or  during  delays 
due  to  other  causes.  When  repairs  were 
made  at  such  times  the  period  occupied  is  es 
timated,  and  marked  with  a  star  (*). 

In  some  instances  the  periods  for  repairs 


and  changes  were  caused  in  part  by  failure  to 
provide  necessary  materials  promptly. 

RECORDS  OF  THE  PERIODS  OCCUPIED  IN  RE 
PAIRS  OF  THE  VARIOUS  DEVICES  OF  THE 
RESPECTIVE  SYSTEMS. 


Device  Repaired. 

Total 

'eriod  Occ 

Jpied. 

Warren. 

Jewell. 

Western. 

*8.0 

*10   8 

0 

*0    - 

Controller  

*2.O 

Inlet  

Ifj.0 

*IO.O 

o*.S 

*IO.O 

RECORDS  OF  THE  PERIODS  OCCUPIED  IN 
CHANGES  OF  THE  VARIOUS  DEVICES  OF 
THE  RESPECTIVE  SYSTEMS. 

Warren. 

1895,  Nov.    12    to   25.      93    hours   30   min 

utes.     Mainly  to  change  sand  layer 
and  modify  filter  tank. 

1896,  Jan.    23    to    25.      20    hours    25    min 

utes.     Mainly  to  change  sand  layer 
and  modify  central  well. 


94 


WATER   PURIFICATION  AT  LOUISVILLE. 


1896,  Feb.  ii  to  13.  19  hours  o  minutes. 
Mainly  to  introduce  auxiliary  wash- 
water  distributing  system,  add  new 
sand  and  raise  central  well. 

Feb.  14.  48  minutes.  Mainly  to 
change  agitator  teeth. 

Feb.  15.  50  minutes.  Mainly  to 
modify  auxiliary  wash-water  distrib 
uting  system. 

Feb.  21.  3  hours  34  minutes.  Mainly 
to  remove  auxiliary  wash-water  dis 
tributing  system,  change  rakes  and 
modify  central  well. 

March  17.  10  minutes.  Mainly  to 
change  position  of  rake-arms. 

April  13  to  20.  59  hours  30  minutes. 
Mainly  to  change  sand  layer  and 
strainer  system. 

April  23.  i  hour  35  minutes.  Mainly 
to  change  agitating  devices. 

April  25.  3  hours  o  minutes.  Mainly 
to  change  agitating  devices. 


1896,  Jan.  31  to  Feb.  4.  26  hours  25  min 
utes.  Mainly  to  change  sand  layer. 

Feb.  14.  47  minutes.  Mainly  to 
change  outlet  valves. 

June  2.  i  hour.  Mainly  to  change 
worm  gear  of  agitator. 

July  3  to  5.  30  hours  o  minutes. 
Mainly  to  change  sand  layer. 

Other  changes  were  made  outside  of  the 
regular  hours  of  operation  at  various  times. 
These  were  mainly  changes  in  chemical  pump, 
lime  apparatus,  other  chemical  devices,  float 
in  main  tank,  chemical  feed-pipe  fittings,  fas 
tenings  for  rake-arms;  the  total  time  so  oc 
cupied  was  about  35  hours. 

Western  Gravity. 

March  22  to  July  2.  765  hours.  During  this 
period  the  main  changes  made  were 
in  the  strainer  floor,  sand  layer, 
wash-water  distributing  systems,  and 
piping  systems. 

The  changes  in  this  filter  were 
complete  on  May  8,  but  the  filter 
was  not  put  in  official  operation  till 
July  2. 


Western  Pressure. 

April  7  to  May  8.  221  hours  45  minutes. 
During  this  period  the  main  changes 
were  made  in  the  devices  for  the  ap 
plication  of  the  chemicals,  the  supply, 
and  the  distributing  piping  systems. 

Records  of  the  Delays  of  Operation  during  the 
Tests. 

In  this  section  is  presented  a  record  of  the 
delays  which  were  met  with,  and  a  summary 
of  the  time  occupied  in  various  ways  during 
these  investigations.  After  the  work  was 
well  begun  it  was  arranged  that  the  systems 
should  be  operated  as  continuously  as  prac 
ticable  from  9.00  A.M.  to  5.30  P.M.  on  each 
week  day,  unless  the  Water  Company  re 
quested  otherwise.  From  March  24,  9.00 
A.M.,  to  March  30,  5.30  P.M.,  the  operations 
were  requested  to  be  continuous,  as  was  the 
case  from  9.00  A.M  on  Monday  to  4.00  P.M. 
on  Saturday  for  each  of  six  weeks  begin 
ning  April  27.  A  number  of  repairs  and 
changes  by  the  operators  of  the  several  sys 
tems,  and  operations  and  observations  by  the 
Water  Company,  reduced  somewhat  the 
available  period  of  operation  as  outlined 
above.  The  chief  factors  which  caused  tie- 
lay  were: 

1.  Repairs   and   Changes. — These    have   al 
ready  been  referred  to  above.     Some  of  the 
principal  ones  necessarily  extended  into  the 
regular    periods    of    operation.      The    minor 
ones  frequently  were  made  outside  the  hours 
of  regular  operations,  as  will  be  noted  from ' 
the    differences    in    total    time    consumed   as 
shown  in  the  first  two  tables  and  in  the  final 
summary. 

2.  Removal  of  Sediment  which  had  Subsided 
to  the  Bottom  of  the  Settling  Chambers. — The 
average  time  required  by  the  respective  sys 
tems  for  this  operation  was  as  follows:   War 
ren,  3  hours;    Jewell,  2  hours;    Western,  6 
hours.     In  a  majority  of  cases  the  settling 
chambers  were  cleaned  at  times  of  washing 
or  when  other  causes  delayed  the  regular  op 
eration  of  these  devices.    The  delays  at  such 
times  were  therefore  less  than  the  actual  time 
required  to  clean  the  chambers.     Exclusive 
of  operations  under  prescribed  conditions,  the 


SUMMARY  OF    THE    VARIOUS  PARTS   OF    THE   SYSTEMS. 


95 


chambers  were  cleaned  on  the  following 
dates: 

Warren  System:  December  19,  1895; 
January  23,  1896;  April  13,  April  28,  June  9, 
July  2,  July  23,  and  July  28. 

Jewell  System:  December  n,  1895;  Feb 
ruary  28,  1896;  April  25,  July  3,  and  July  17. 

Western  System:  December  31,  1895; 
January  13,  1896;  April  7,  June  3,  June  8, 
June  24,  and  July  23. 

3.  Sterilization    of   the   Sand   La\cr. — This 
occurred  three  times  in  the  case  of  the  Jewell 
System,   on    October   30,    1895;    January   8, 
1896;  and  February  28,   1896.     About  four 
hours  were  required  for  the  operation  each 
time,  and  the  sand  was  allowed  to  cool  over 
night.    Sterilization  was  not  attempted  in  any 
of  the  other  systems. 

4.  Change  of  Water  in  Settling  Chambers. — 
This  was  occasioned  in  some  instances  by  the 
conditions    prescribed    by    the    Water    Com 
pany    during    the    period    from    May    18    to 
June  6.    The  water  was  usually  changed  dur 
ing  the  time  of  washing  the  niters  in  order  to 
make  the  delay  as  small  as  possible.      The 
periods  required  for  the  operation  depended 
on  the  rate  which  was  being  maintained  and 
the  size  of  the  respective  settling  chambers. 


The  dates  when  these  operations  took  place 
were: 

Warren  System:  May  18,  19,  20,  21,  25,  27, 
28,  and  29;  June  i,  2,  and  4. 

Jewell  System:  May  18,  19,  22,  26,  28,  29, 
and  30;  June  2,  4,  and  5. 

Western  Pressure  System:  May  28,  29,  and 
June  4. 

5.  Observations  and  Operations  b\  the 
Water  Company. — These  included  inspection 
of  systems,  collection  of  sand  samples,  special 
tests,  repairs  of  meters  and  pipes,  and  ex 
amination  of  various  details.  The  total 
periods  of  delay  were:  Warren,  33.2  hours; 
Jewell,  56.2  hours;  Western  Gravity,  15.6 
hours;  Western  Pressure,  22.6  hours. 

The  following  table  gives  a  summary  of  the 
total  periods  available  for  operation  of  each 
system,  the  periods  during  which  the  respec 
tive  systems  were  in  actual  operation,  and  the 
periods  during  which  the  above-mentioned 
causes  of  delay  interfered  with  the  regular 
operation  of  the  systems. 

It  is  to  be  noted  that  in  this  table  the  actual 
total  time  used  in  operation  is  presented, 
while  in  the  final  summary  in  Chapter  IX 
only  the  period  occupied  by  operations  in 
cluded  in  averages  is  given. 


SUMMARY    OF   THE    TIME    OCCUPIED    IN   VARIOUS    WAYS    DURING    THE   TESTS    IN    DAYS    OF 

24    HOURS. 


Warren. 

Jewell. 

Western 

Gravity. 

Pressure 

Oct.  21,  '95 
Aug.  i,  'i/> 
103.56 
91  .63 
i  .09 
8.40 

O.2I 

Oct.  21,  '95 

Aug.  i,  '96 
102.54 
94.00 
0.79 
3-89 
0.16 

Dec.  23/95 
Aug.  i,  '96 
65-45 
26.50 

0. 

31.88 
0.05 

Dec.  23,  '95 
Aug    i,  '96 
79.46 
66.05 
o.  10 
9.25 
0.05 
0.03 
0.94 
o 

2.12 
O.92 

Pe  iod  available  for  operation  (by  arrangement)      

Pe  iod  used  for  repairs   

Period  used  to  change  water  in  settling  chambers  

L38 
0. 

o. 

0.  10 

2.34 
0.50 
o. 
0.34 

0.65 

0. 

5.67 

0.70 

Period  used  for  sterilizing  sand  layer  

Periods  when  by  request  of  Filter  Company  systems  were  out  of  service  .... 

WATER   PURIFICATION  AT  LOUISVILLE. 


CHAPTER  VII. 

THE  MANNER  OF  OPERATION  OF  THE  RESPECTIVE  SYSTEMS  OF  PURIFICATION  AND  THE 
AMOUNT  OF  ATTENTION    GIVEN  THERETO. 


THE  method  of  water  purification  investi 
gated  in  these  tests,  generally  called  up  to  this 
time  "  mechanical  filtration,"  has  been  held  by 
some  to  be  so  simple  that  practically  no  atten 
tion  is  required  for  its  satisfactory  operation. 
To  many,  however,  the  name  conveys  a  dif 
ferent  impression,  that  of  a  mechanism  or 
combination  of  mechanical  devices,  for  the 
perfect  working  of  which,  like  that  of  any 
other  appliance,  careful  and  systematic  su 
pervision  must  be  maintained. 

It  is  the  purpose  of  this  chapter  to  show 
that  the  latter  supposition  is  correct  so  far  as 
it  relates  to  the  purification  of  the  unsettled 
Ohio  River  water,  because  for  the  efficient 
maintenance  of  the  systems  examined  during 
these  tests  constant  care  and  regulation  were 
necessary;  and,  further,  that  without  this,  ir 
regularities,  often  highly  detrimental  both  to 
the  character  of  the  effluent  and  the  cost  of 
treatment,  were  bound  to  occur. 

The  following  topics  will  be  presented  in 
this  connection: 

1.  The  general  manner  of  operation  of  the 
different  systems. 

2.  The    mechanical    devices    installed    and 
used  to  aid  in  the  operation  of  the  systems. 

3.  The    attention    given    to    the    systems 
throughout  the  tests. 

Under  section  No.  i  will  be  presented  a 
general  outline  of  the  manner  of  operation  of 
the  different  parts  of  the  respective  systems. 

Section  No.  2  includes  a  detailed  descrip 
tion  of  the  special  valves  and  other  devices 
used  to  regulate  or  control  the  different  op 
erations.  These  have  already  been  referred 
to  briefly  under  the  different  portions  of 
Chapters  II,  IV.  and  V. 

Section  No.  3  will  include  statements  of  the 
number  of  men  employed  by  each  system 
throughout  the  test. 


THE  GENERAL  MANNER  OF  OPERATION  OF 
THE  RESPECTIVE  SYSTEMS. 

The  general  manner  of  operation  of  all  the 
systems  represented  at  these  tests  may  be  de 
scribed  as  follows: 

1.  The  treatment  of  the  river  water  with 
alum  or  sulphate  of  alumina  for  the  purpose 
of  obtaining  coagulation  and  subsequent  sedi 
mentation. 

2.  The  filtration  of  the  coagulated  water, 
partially  purified  by  sedimentation,  through  a 
layer  of  sand. 

3.  The  washing  of  the  filter  (sand  layer). 

Nos.  i  and  2  were  carried  on  simulta 
neously,  but  were  quite  separate  in  their 
methods  of  control. 

In  the  following  pages  these  different  op 
erations  for  the  respective  systems  will  be 
described  in  order. 

Operation  of  the  Warren  System. 

Application  of  Sulphate  of  Alumina. — The 
river  water  was  supplied  under  pressure  to  the 
Warren  System  through  a  5-inch  pipe  which 
was  enlarged  to  6  inches  at  the  settling  basin. 
The  passage  of  the  water  through  this  pipe 
was  controlled  by  a  5-inch  gate  valve,  and  a 
6-inch  balanced  valve  on  the  mouth  of  the  in 
let  pipe,  the  balanced  valve  being  operated  by 
a  float  in  the  settling  basin.  As  has  already 
been  described  in  Chapter  II,  the  arrange 
ment  used  for  the  application  of  the  sulphate 
of  alumina  solution  comprised  a  propeller 
wheel  in  the  mouth  of  the  inlet  pipe;  a  pump 
on  the  upper  floor  operated  by  the  propeller 
wheel :  and  a  pair  of  tanks  in  which  the  solu 
tion  was  made,  and  from  which  it  flowed  by 
gravity  to  the  pump  box. 

The   operation   of  the  whole   device   was 


MANNER   OF  OPERATION  OF    THE  PURIFICATION  SYSTEMS. 


91 


automatic,  as  the  current  of  water  upon  enter 
ing  the  basin  operated  the  propeller;  and  it  ii 
turn  drove  the  pump,  to  which  the  solutior 
flowed  from  the  chemical  tanks  by  gravity. 

For  the  successful  operation  of  this  portion 
of  the  system,  regulation  of  the  rate  of  inflow 
of  the  river  water  was  required.  Control  ol 
the  strength  solution  was  also  required.  The 
amount  of  sulphate  of  alumina  applied  to  the 
water  was  regulated  in  two  ways: 

1.  By  varying  the  strength  of  solution. 

2.  By  varying  the  number  of  arms  on  the 
pump  into  which  stoppers  were  inserted,  to 
prevent  the  entrance  of  the  solution  into  the 
arms.    This  is  more  fully  described  in  Chap 
ter  II. 

It  will  be  seen  that  the  design  of  this  por 
tion  of  the  system  called  only  for  the  initial 
application  and  the  regulation  of  the  river 
water  into  the  settling  basin,  by  hand;  atten 
tion  to  the  preparation  of  the  sulphate  of 
alumina  solution;  and  the  adjustment  of  the 
[jump  to  deliver  a  suitable  quantity  of  chemi 
cals.  The  balance  of  the  work  was  automatic. 
The  special  construction  of  the  automatic  de 
vices  will  be  described  in  the  next  section. 

From  the  settling  basin  the  water  passed 
through  a  pipe  to  the  central  well  of  the  filter, 
and  thence  to  the  top  of  the  sand. 

Filtration. — Starting  with  a  clean  sand  layer 
just  after  washing,  the  settling  basin  full  of 
chemically  treated  water,  and  all  valves  closed, 
the  first  operation  was  to  open  a  valve  on  the 
inlet  pipe  from  the  settling  basin  to  the  filter, 
allow  the  water  to  fill  the  central  well,  over 
flow  on  top  of  the  sand  and  slowly  rise  in  the 
open  compartment  above  the  sand.  It  was 
necessary  to  let  the  filter  fill  slowly  to  avoid 
disturbance  of  the  sand  surface.  From  8  to 
15  minutes  were  occupied  in  filling  the  filter, 
the  average  time  being  about  10  minutes.  As 
soon  as  the  water  reached  within  about  0.5 
foot  of  the  maximum  level,  a  valve  on  the 
waste  pipe  was  opened  slowly  and  filtration 
begun.  At  the  same  time  the  valve  on  the  in 
let  pipe  to  the  filter  was  opened  wide.  Dur 
ing  the  latter  and  greater  portion  of  the  tests 
no  water  was  wasted  in  this  system  following 
a  wash  of  the  filter,  and  the  filtered  water  was 
turned  immediately  into  the  main  outlet  pipe 
leading  to  the  weir  box.  When  wasting  was 
practiced  the  rate  of  flow  of  water  was  regu- 


lated  by  hand  by  means  of  a  4-inch  gate  valve 
on  this  pipe.  When  the  water  became  satis 
factory  in  appearance,  the  valve  in  the  waste 
pipe  was  closed,  and  a  valve  on  the  main  out 
let  pipe,  leading  to  the  weir  box,  opened. 
This  valve  was  opened  slowly,  allowing  the 
filtered  water  to  enter  the  weir  box  and  rise 
on  the  inlet  side  thereof.  As  soon  as  the 
water  began  to  flow  over  the  crest  of  the  weir, 
the  valve  on  the  outlet  pipe  was  opened  wide, 
and  the  rate  of  filtration  regulated  by  means 
of  the  weir.  The  entire  system  was  then  in 
operation.  The  water  was  treated  with  suU 
phale  of  alumina  as  it  entered  the  settling 
basin  through  which  it  flowed  on  its  way  to 
the  sand  layer.  After  it  was  filtered,  it  was 
discharged  over  the  weir. 

The  rate  of  flow  of  water  through  the  en 
tire  system  was  regulated  solely  by  the  mova 
ble  weir,  which  was  used  only  for  this  pur 
pose  and  not  as  a  measuring  device.  The 
height  of  this  weir  was  adjusted  at  varying  in 
tervals,  depending  largely  on  the  amount  of 
suspended  matter  in  the  water  flowing  into 
the  filter.  As  a  general  rule,  at  intervals  of 
half  or  three  quarters  of  an  hour  it  was  low 
ered  an  amount  necessary  to  maintain  the  de 
sired  rate  of  filtration,  the  meter  on  the  pipe 
from  the  weir  chamber  to  the  filtered-water 
reservoir  being  used  for  the  determination  of 
the  actual  rate. 

During  filtration  the  water  passed  freely 
from  the  settling  basin  to  the  compartment  at 
the  top  of  the  filter,  and  stood  at  the  same 
level  in  each. 

When  it  was  considered  necessary  to  waste 
the  filtered  water  during  filtration,  the  valve 
on  the  pipe  connecting  the  filtered-water 
chamber  beneath  the  filter  and  weir  box  was 
closed,  and  the  valve  on  the  waste  pipe 
opened,  the  rate  of  flow  of  water  being  regu 
lated  by  hand.  When  the  effluent  became 
clear,  the  change  was  made  to  the  main  outlet 
pipe  as  described  above  in  starting  filtration. 
If  the  effluent  did  not  become  clear  in  a  rea 
sonable  length  of  time  the  filter  was  prepared 
or  washing  in  the  manner  described  below. 

Decision  to  IVasli  the  Filter. — This  decision 
was  one  which  required  considerable  judg- 
nent.  During  the  whole  test  no  case  was  re 
corded  where  the  Warren  filter  was  washed 
on  account  of  the  entire  available  head  having 


WATER  PURIFICATION  AT  LOUISVILLE. 


been  used,  and  the  rate  falling  below  the  de 
sired  quantity.  In  fact,  less  than  60  per  cent, 
of  the  available  head  obtained  with  the  weir 
(4.17  feet)  was  ordinarily  utilized.  In  general 
it  may  be  said  that  the  only  immediate  guide 
to  the  decision  to  wash  the  filter  at  any  par 
ticular  time  was  the  appearance  of  the  efflu 
ent. 

In  passing  it  may  be  stated,  further,  that 
the  decision  as  to  washing  was  influenced  in 
a  measure  by  several  other  features,  the  rela 
tive  importance  of  which  varied  from  time  to 
time.  These  features  related  largely  to  the 
quality  of  the  river  water  as  it  flowed  from  the 
settling  basin  to  the  filter,  and  especially  in 
connection  with  the  relative  amount  of 
aluminum  hydrate  present  in  the  water  at  that 
point.  The  significance  of  these  features  will 
be  mentioned  beyond. 

Preparations  for  Washing  the  Filter. — When 
it  was  decided  to  wash  the  filter  the  valve  on 
the  inlet  pipe  to  the  filter  from  the  settling 
basin  was  closed.  The  water  above  the  sand 
was  then  allowed  to  filter  off  through  the 
sand,  the  rate  being  carefully  regulated  to  the 
normal  in  order  to  maintain  as  good  a  charac 
ter  of  effluent  as  possible.  This  was  continued 
until  the  water  was  drained  down  as  far  as  de 
sired.  With  the  use  of  the  weir  alone,  there 
was  left  at  least  2  feet  of  water  above  the 
sand.  By  the  introduction  of  the  valve  (Feb. 
12)  in  the  weir  chamber  further  drainage  was 
made  possible,  only  about  0.5  foot  of  water 
being  left  above  the  sand  when  this  valve  was 
used.  During  draining  the  settling  basin  was 
allowed  to  fill  till  the  float  closed  the  valve  on 
the  inlet  pipe. 

Washing  of  the  Filter. — During  the  drain 
ing  of  the  filter,  preparatory  to  washing,  the 
engine  used  for  operating  the  agitator 
machinery  was  "  warmed  up."  As  soon  as 
the  filter  was  drained,  the  engine  was  started 
at  full  speed  and  the  friction-clutch  of  the  agi 
tator  engaged.  This  started  the  agitator, 
which  was  allowed  to  turn  a  partial  revolu 
tion  before  the  lowering  gear  was  engaged. 
The  agitator  then  slowly  descended,  revolving 
at  the  same  time.  After  about  one  revolution 
the  wash-water  \vas  admitted  into  the  filtered- 
water  chamber  at  the  bottom  of  the  filter. 
The  pressure  of  the  water  forced  it  up  through 


the  perforated  bottom  into  and  through  the 
sand  layer,  thus  loosening  the  sand.  The  agi 
tator  continued  to  descend  until  it  reached  the 
full  depth  into  the  sand,  when  a  system  of 
levers  automatically  disengaged  the  lowering 
gears.  At  times  these  gears  were  thrown  so 
far  that  the  raising  gears  were  engaged,  neces 
sitating  adjustment  by  hand. 

Washing  was  continued  till  the  sand  was, 
in  the  opinion  of  the  operator,  cleansed  suf 
ficiently.  During  this  time  the  power  given 
to  the  agitator  machinery  was  left  constant, 
and  the  amount  of  wash-water  admitted  was 
regulated  so  as  to  maintain  a  regular  rate  of 
revolution  of  the  agitator,  usually  from  six  to 
eight  revolutions  per  minute.  The  rate  of  ad 
mission  of  wash-water  was  regulated  by  a  valve 
operated  by  hand.  The  maximum,  minimum, 
and  average  vertical  velocities  of  the  wash- 
water  used  (estimating  45  per  cent,  of  the  sand 
layer  occupied  by  water)  were  4.05,  0.86,  and 
1.79  linear  feet  per  minute,  respectively. 

As  soon  as  the  bed  was  cleansed  to  the  de 
sired  degree,  the  lifting  gears  were  engaged 
and  the  rakes  raised  out  of  the  sand.  It  was 
customary  at  this  time  to  supply  a  little  more 
steam  to  the  engine  and  to  admit  a  little  extra 
wash-water,  as  the  greatest  load  came  on  the 
agitating  machinery  when  lifting  the  rakes. 
The  construction  of  the  machinery  was  such 
that  the  rakes  could  not  be  lifted  vertically 
out  of  the  sand,  but  must  continue  to  revolve 
while  rising.  As  the  rakes  approached  their 
highest  position,  steam  was  gradually  shut  off 
from  the  engine.  For  some  time  it  was  cus 
tomary  to  shut  off  the  wash-water  when  the 
rakes  were  about  three-fourths  out  of  the 
sand.  In  the  early  part  of  February,  however, 
it  was  found  that  by  continuing  the  supply  of 
wash-water  till  the  agitator  was  fully  raised 
and  stopped,  the  ridges  in  the  sand  formed 
by  the  rake-teeth  were  lessened.  After  this 
date  it  was  customary  to  shut  off  the  wash- 
water  gradually  as  the  rakes  ascended,  to  stop 
the  agitator  by  disengaging  the  friction- 
clutch  as  soon  as  the  rakes  were  fully  raised, 
and  then  to  shut  off  the  wash-water  entirely. 
The  engine  was  then  stopped. 

The  filter  was  now  ready  for  filling  with 
water  from  the  settling  basin  preparatory  to 
filtration,  as  has  been  described. 


MANNER   OF  OPERATION   OF    THE  PURIFICATION  SYSTEMS. 


Operation  of  the  Jewell  System. 

The  same  method  of  presentation  of  the 
operation  of  this  system  will  be  followed  as 
was  used  with  the  Warren  System. 

Application  of  Sulphate  of  Alumina. — The 
river  water  was  supplied  to  the  Jewell  System, 
under  a  pressure  of  about  60  pounds,  through 
a  5-inch  pipe.  The  pipe  through  which  the 
solution  of  sulphate  of  alumina  was  pumped 
joined  the  inlet  pipe  at  a  point  about  10  feet 
from  the  entrance  to  the  settling  chamber. 
The  river  water  and  chemical  solution  had  to 
pass  through  the  inlet  meter  and  two  valves 
before  they  reached  the  settling  chamber. 

Two  valves  (a  hand  valve  and  an  automatic 
valve)  were  used  to  control  the  flow  through 
the  inlet  pipe.  The  first  was  a  simple  globe 
valve  used  to  regulate  the  flow  when  starting 
the  system  or  to  shut  off  the  river  water  upon 
stopping  operations.  The  other  valve  was 
situated  in  the  mouth  of  the  inlet  pipe  within 
the  settling  chamber.  It  was  controlled  by  a 
float  in  the  compartment  above  the  sand  in 
the  filter,  and  was  relied  upon  to  regulate 
the  rate  of  admission  of  the  water  into  the 
system  as  soon  as  the  water  rose  high  enough 
to  set  the  float  in  operation.  Regulation  of 
the  rate  of  admission  of  the  water  to  the 
settling  chamber  also  controlled  its  passage 
through  the  chamber  and  entrance  to  the  fil 
ter. 

The  rate  of  application  of  the  chemicals  to 
the  river  water  was  regulated  solely  by  the 
speed  of  the  pump  used  for  that  purpose.  For 
large  changes  in  the  amount  of  chemicals  ap 
plied  to  the  water,  the  strength  of  the  solu 
tion  was  varied.  The  speed  of  the  pump  was 
adjusted  by  regulation  of  a  steam  throttle- 
valve,  the  pressure  of  the  steam  being  held 
nearly  constant  by  a  regulating  valve  on  the 
main  steam-pipe.  During  the  early  part  of 
the  test,  the  throttle-valve  on  the  pump  for 
the  delivery  of  sulphate  of  alumina  was  con 
trolled  by  a  float  at  the  top  of  the  filter.  This 
was  found  to  be  unsatisfactory  and  hand  regu 
lation  was  relied  upon  throughout  the  balance 
of  the  test.  The  rate  of  feeding  the  sulphate 
of  alumina  solution  for  short  intervals  was  de 
termined  by  counting  the  strokes  of  the 
pump,  the  delivery  of  which  was  approxi 
mately  2.1  cubic  inches  per  stroke.  For 


longer  periods  control  was  obtained  by  com 
parison  of  the  readings  of  the  meter  used  for 
measuring  the  amount  of  solution  and 
the  meter  on  the  inlet  water-pipe.  To  start  or 
stop  the  application  of  the  sulphate  of  alumina 
solution  the  throttle-valve  was  opened  or 
closed.  The  chemical  pump  was  started  just 
before  the  valve  on  the  inlet  water-pipe  was 
opened,  and  stopped  immediately  after  the 
latter  was  closed.  A  check-valve  on  the 
chemical  feed  pipe  prevented  the  flow  of 
water  through  this  pipe  from  the  inlet  water- 
pipe  when  the  pump  was  stopped. 

It  will  be  noted  that  the  regulation  of  the 
entrance  of  river  water  was  automatic,  but 
that  the  regulation  of  the  application  of  the 
sulphate  of  alumina  required  adjustment  by 
hand  of  the  throttle-valve  of  the  pump. 

The  application  of  the  mixed  lime  and  sul 
phate  of  alumina  was  regulated  at  first  in  the 
same  manner  as  the  application  of  sulphate 
of  alumina,  one  pump  being  used  for  the  de 
livery  of  both  solutions. 

No  adequate  means  were  provided  to  regu 
late  the  relative  quantities  of  the  two  solu 
tions.  This  was  remedied  in  the  latter  part 
of  March  by  the  use  of  an  entirely  separate 
arrangement  for  delivering  the  lime,  includ 
ing  a  separate  pump  and  piping  system. 

Filtration. — The  water  after  passing  through 
the  settling  chamber  rose  up  through  the  cen 
tral  well  and  overflowed  in  the  compartment 
of  the  filter  above  the  sand.  Its  flow  was 
regulated  by  the  entrance  of  the  river  water 
into  the  settling  chamber,  and  this  in  turn 
was  controlled  for  the  most  part  by  the  float 
valve  described  above. 

Starting  with  a  clean  sand  layer  just  after 
washing,  the  settling  chamber  filled  with 
chemically  treated  water,  and  all  valves 
closed,  filtration  was  proceeded  with  as  fol 
lows: 

The  valve  on  the  inlet  water-pipe  leading 
to  the  settling  chamber  was  first  opened  and 
the  sulphate  of  alumina  pump  started.  This 
caused  the  water  to  rise  in  the  central  well 
and  overflow  on  top  of  the  sand  in  the  filter. 
As  soon  as  the  water  had  reached  its  normal 
height  above  the  sand,  the  outlet  was  opened, 
and  filtration  begun.  This  process  of  filling 
the  filter  usually  occupied  about  6  minutes, 
the  time  being  dependent  upon  the  rate  used. 


WATER   PURIFICATION  AT  LOUISVILLE. 


In  filling  the  filter  the  rate  of  flow  was  regu 
lated  by  hand  to  the  required  amount,  as  the 
float  valve  did  not  operate  unless  the  water 
was  almost  at  its  normal  height  in  the  filter. 

As  the  main  outlet  pipe  and  the  waste-water 
pipe  were  simply  different  branches  of  the 
same  pipe  leading  from  the  manifold  in  which 
the  filtered  water  was  collected  beneath  the 
sand,  no  special  difference  in  the  operation 
occurred  whether  the  main  outlet  pipe  or 
waste  pipe  was  used.  It  was  customary  in 
this  system  to  turn  the  filtered  water  directly 
into  the  main  outlet  pipe.  This  operation 
will  therefore  be  described  next. 

The  flow  through  the  main  outlet  pipe  was 
controlled  by  a  valve  operated  by  hand,  which 
was  supplemented  during  the  latter  portion  of 
the  test  by  an  automatic  controller.  In  start 
ing  filtration  this  valve  was  opened  and  the 
rate  of  flow  regulated  to  the  desired  quantity. 
This  was  the  only  means  of  regulating  the  rate 
of  filtration  up  to  April  10,  when  the  auto 
matic  controller  was  introduced.  This  device, 
which  will  be  described  in  the  next  section, 
was  so  arranged  that  a  variation  in  the  flow 
through  it  closed  a  valve  automatically,  if  the 
flow  increased,  or  opened  it  if  the  flow  de 
creased.  After  the  introduction  of  this  de 
vice,  it  was  customary  to  open  wide  the  valve 
on  the  main  outlet  pipe  as  soon  as  the  con 
troller  was  in  operation.  Owing  to  the  pres 
sure  required  to  operate  this  controller,  the 
head  available  for  filtration  was  reduced  about 
4  feet.  To  obviate  this  difficulty  there  was 
placed  on  the  main  outlet  pipe  a  by-pass 
which  cut  out  the  controller.  This  by-pass 
was  used  when  the  available  head  fell  below 
that  necessary  when  the  controller  was  in  op 
eration.  Under  such  circumstances  the  valve 
on  the  main  outlet  pipe  was  used  to  regulate 
the  rate  of  filtration  by  hand. 

Whenever  it  was  considered  necessary  to 
waste  the  filtered  water,  the  valve  on  the  main 
outlet  pipe  was  closed  and  the  valve  on  the 
waste  pipe  opened,  the  rate  of  flow  being  ad 
justed  by  hand. 

Filtration  was  continued  until  one  of  the 
two  following  conditions  appeared:  either 
the  resistance  of  the  filter,  due  to  accumula 
tions  of  matters  removed  from  the  water,  be 
came  so  great  that  the  desired  rate  could  not 
be  maintained  with  the  available  head,  or  the 


appearance  of  the  effluent  became  unsatisfac 
tory  in  the  opinion  of  the  operator. 

The  determination  of  the  course  to  be  pur 
sued  under  these  circumstances  rested  with 
the  judgment  of  the  operator  of  the  system. 
At  times  it  was  found  that  the  appearance  of 
the  effluent  might  fail  for  a  short  period  and 
then  improve.  Wasting  the  effluent  for  a 
short  time  was  often  tried  under  these  condi 
tions.  When  the  available  head  fell  below 
that  necessary  to  maintain  the  desired  rate  of 
flow,  one  of  the  two  following  operations  was 
adopted:  either  the  filter  was  washed  or  the 
surface  of  the  sand  agitated. 

Surface  agitation  consisted  in  trailing  the 
agitator  (generally  by  hand)  in  a  reverse  di 
rection  for  about  one  revolution.  By  this 
means  the  surface  of  the  sand  was  disturbed 
by  the  rake-teeth  which  rested  upon  it,  and 
the  layer  of  sediment  on  the  top  of  the  sand 
was  broken  up  more  or  less.  During  this  op 
eration  the  passage  of  water  through  the  sys 
tem  was  stopped,  but  the  water  above  the 
sand  was  never  removed.  Application  and 
filtration  of  the  water  were  immediately  re 
sumed,  the  whole  operation  occupying  from 
i  to  3  minutes.  Several  times  during  the 
early  part  of  the  test  continuous  agitation  of 
the  surface  of  the  sand  during  filtration  was 
tried.  It  cannot  be  said  to  have  been  a  nor 
mal  procedure,  however. 

In  deciding  whether  to  agitate  the  surface 
of  the  sand  or  to  wash  the  filter,  many  con 
siderations  had  to  be  borne  in  mind. 

Decision  to  Agitate  the  Surface  of  tlic  Sand. 
— With  a  decreasing  rate  of  flow,  owing  to 
increasing  resistance  of  the  filter,  and  a  satis 
factory  appearance  of  the  filtered  water,  the 
question  as  to  whether  it  was  better  to  agitate 
the  surface,  or  wash  the  filter,  involved  a  con 
sideration  by  the  operator  of  the  following 
factors: 

1.  Length  of  the  last  run  and  amount  of 
water  filtered  during  the  same. 

2.  Cause  for  last  wash. 

3.  Success  of  surface  agitation  on  last  run, 
if  tried. 

4.  Length  of  present  run  and  amount  of 
water  filtered. 

5.  Appearance  of  the  water  flowing  from 
the    settling    chamber    to    the    top    of    the 
filter. 


MANNER   OF  OPERATION  OF    THE  PURIFICATION  SYSTEMS. 


It  was  found  that  under  some  conditions 
two  and  sometimes  three  surface  agitations 
between  washings  were  successful;  while  at 
other  times  the  disturbance  of  the  surface 
caused  a  deterioration  in  the  character  of  the 
effluent,  which  did  not  improve.  The  degree 
of  coagulation  of  the  water  as  it  entered  the 
sand  layer  seemed  to  be  a  controlling  factor. 

Decision  to  Wash  the  Filter. — Several  factors 
influenced  this  decision,  which  was  in  general 
only  reached  after  a  careful  study  of  the  vary 
ing  conditions  under  which  the  system  was 
being  operated.  Unsatisfactory  appearance 
of  the  effluent  and  a  utilization  of  the  total 
available  head  were  the  immediate  guides  to 
washing.  The  quality  of  the  river  water  be 
fore  and  after  filtration,  as  shown  by  inspec 
tion  and  analytical  results,  was  an  important 
factor. 

Preparations  for  Washing  the  Filter. — When 
it  was  decided  to  wash  the  filter  the  valve  on 
the  inlet  water-pipe  was  closed,  the  chemical 
pump  stopped,  and  the  water  above  the  sand 
allowed  to  filter  off.  When  the  water,  in  the 
opinion  of  the  operator,  was  seriously  defi 
cient  in  quality  it  was  drained  out  through 
the  waste  pipe  for  filtered  water  or  drawn  off 
from  above  the  sand  by  means  of  the  collect 
ing  gutter  which  connected  with  a  pipe  lead 
ing  to  the  sewer.  As  a  rule,  however,  the 
water  while  draining  the  filter  was  allowed 
to  pass  into  the  main  outlet  pipe  to  the  fil- 
tered-water  reservoir.  During  the  draining 
of  the  filter  the  engine  used  for  driving  the 
agitator  was  "  warmed  up." 

Washing  the  Filter. — As  soon  as  the  water 
above  the  sand  was  drained  off,  the  engine 
was  started  at  full  speed  in  reverse  motion. 
The  wash-water  was  then  turned  into  the  out 
let  pipe  and  allowed  to  force  its  way  up 
through  the  sand.  As  soon  as  it  appeared 
on  the  surface  of  the  sand  (generally  about 
i  minute)  the  engine  was  reversed,  and  the 
rake-teeth  turning  on  the  arms  penetrated 
the  sand  to  their  full  available  length.  The 
agitator  was  continued  in  operation,  stirring 
the  sand  throughout  the  wash.  Up  to  May 
i  the  rate  of  delivery  of  the  wash-water  was 
regulated  to  maintain  a  certain  pressure  on 
the  sand.  After  this  date  the  valve  on  the 
wash-water  pipe  was  left  wide  open  during 
washing.  The  agitator  was  operated  nor 


mally  at  a  speed  of  eight  to  nine  revolutions 
per  minute. 

Washing  was  continued  until  the  sand  layer 
was  cleansed  sufficiently,  in  the  opinion  of  the 
operator,  when  the  valve  on  the  wash-water 
pipe  was  closed.  The  agitator  engine  was 
immediately  reversed,  and  the  rake-teeth  were 
thrown  to  the  surface  by  the  resistance  of  the 
sand,  which  very  quickly  settled  into  place. 
The  engine  was  then  stopped. 

In  washing  this  filter  the  wash-water  was 
passed  upward  through  the  sand  layer  (esti 
mating  45  per  cent,  of  the  layer  as  occupied  by 
water)  at  the  following  vertical  velocities  in 
linear  feet  per  minute:  Maximum,  2.58; 
minimum,  0.42;  average,  1.37. 

Operation  of  the  Western  Systems. 

The  arrangement  of  the  Western  Systems, 
as  has  already  been  stated,  was  such  that  the 
supply  of  river  water,  the  apparatus  for  the 
application  of  alum  or  sulphate  of  alumina, 
and  the  settling  chamber  were  used  by  both 
filters  in  common.  The  first  portion  of  the 
description  will  therefore  apply  to  both  the 
gravity  and  pressure  systems. 

Application  of  Alum — Original  Device. — In 
the  original  device  the  river  water  was  sup 
plied  under  pressure  through  a  6-inch  pipe 
leading  directly  to  the  settling  chamber.  The 
flow  of  water  through  this  pipe  was  controlled 
by  a  valve  operated  by  hand.  From  this  pipe, 
on  each  side  of  the  valve,  a  small  brass  pipe 
led  to  the  alum  tank.  The  inlet  pipe  to  the 
tank,  from  the  upper  side  of  the  valve,  passed 
through  the  cover  of  the  tank,  and  projected 
into  it  about  I  foot.  The  outlet  pipe  simply 
passed  through  the  cover  of  the  alum  tank 
and  entered  the  inlet  water-pipe  below  the 
valve.  This  tank  was  water-tight,  and  in  it 
were  placed  crystals  of  potash  alum.  After 
the  addition  of  the  alum  the  cover  was  re 
turned,  and  the  water  from  the  main  inlet 
water-pipe  was  admitted  to  the  alum  tank 
through  the  small  brass  inlet  pipe.  A  valve 
was  placed  on  each  of  the  brass  pipes  to  regu 
late  the  flow  through  them. 

To  start  the  supply  of  river  water  and  alum 
solution  to  the  settling  chamber,  the  valve  on 
the  inlet  water-pipe  was  opened  nearly  wide, 
but  not  completely  so,  thus  leaving  a  differ- 


WATER  PURIFICATION  AT  LOUISVILLE. 


ence  in  pressure  on  the  two  sides  of  the  valve. 
The  valve  on  the  brass  pipe  leading  to  the 
alum  tank  was  normally  left  open.  When  the 
valve  on  the  inlet  water-pipe  was  opened,  the 
valve  on  the  brass  pipe  leading  from  the  alum 
tank  to  the  inlet  water-pipe  was  also  opened. 
The  difference  in  pressure  caused  a  current  of 
water  to  pass  from  the  inlet  water-pipe 
through  the  alum  tank  and  back  to  the  inlet 
water-pipe.  It  was  considered  that  this  water 
in  passing  through  the  alum  tank  formed  a 
saturated  alum  solution.  The  rate  of  flow  of 
this  solution  was  regulated  by  hand,  the  valve 
on  the  brass  outlet  pipe  from  the  alum  tank 
being  used  for  this  purpose.  The  actual  rate 
of  flow  was  observed  by  the  aid  of  a  small 
meter.  No  regulation  of  the  water  entering 
the  settling  chamber  was  attempted,  as  the 
rate  of  entrance  of  water  was  controlled  solely 
by  the  rate  of  removal  of  water  from  the  set 
tling  chamber,  which  was  kept  constantly 
rilled  and  under  nearly  the  full  pressure.  The 
water  passed  through  the  settling  chamber 
and  out  at  the  top  into  the  chamber  outlet 
pipe,  w.hich  branched  in  front  of  the  chamber 
into  a  supply  pipe  for  the  gravity  filter  and 
a  supply  pipe  for  the  pressure  filter. 

Unless  the  whole  system  was  taken  out  of 
operation  for  a  time  no  change  was  made  in 
the  valves  on  the  main  inlet  pipe  at  all,  except 
to  regulate  the  rate  of  application  of  alum  as 
described  above. 

Application  of  Alum  or  Sulphate  of  Alumina 
— Second  Device. — As  has  been  described  in 
Chapter  II,  the  second  device  used  in  this 
system  for  the  treatment  of  the  river  water 
with  alum  or  sulphate  of  alumina  consisted 
mainly  of  two  mixing  tanks  and  a  pair  of  small 
pumps,  together  with  suitable  piping. 

The  arrangement  of  the  inlet  pipes  was 
changed  but  little  so  far  as  general  operation 
is  concerned.  Unless  the  system  was  to  be 
taken  out  of  operation,  the  river  water  had 
free  passage  into  the  settling  chamber  at  all 
times.  The  only  change  in  this  portion  of 
the  system  was  the  operation  of  the  main 
water  pump.  As  soon  as  the  valve  on  the 
pipe  leading  from  the  settling  chamber  to 
either  filter  was  opened,  and  the  water  drawn 
from  the  settling  chamber,  the  pump  was 
started  in  operation  by  opening  the  steam 
throttle-valve.  This  valve  was  opened  to 


a  regular  position  and  allowed  to  remain 
there  till  the  draft  on  the  settling  chamber 
was  stopped,  when  the  pump  slowed  down 
owing  to  the  increased  pressure  to  pump 
against.  The  throttle-valve  was  then  closed. 

The  device  for  the  application  of  alum  or 
sulphate  of  alumina  was  put  in  operation 
simultaneously  with  the  main  water  pump, 
as  the  chemical  pumps  were  simple  extensions 
of  the  piston-rods  of  the  water  pumps.  When 
starting,  the  valves  cutting  off  the  supply  of 
chemical  solution  from  the  tanks  to  the  pumps 
were  opened,  the  air  in  the  pumps  blown  off 
by  means  of  petcocks,  and  the  device  was 
then  in  operation. 

The  method  of  regulation  of  the  chemical 
application,  as  in  the  Warren  and  Jewell  sys 
tems,  was  either  by  changes  in  the  strength 
of  solutions,  or  by  varying  the  rate  of  applica 
tion.  Setting  aside  leakages,  the  discharge 
from  the  chemical  pumps  was  practically  con 
stant.  The  method  used  to  control  the  rate 
of  application  was  to  regulate  by  hand  the 
rate  of  return  from  the  pumps  to  the  mixing 
tanks  of  a  portion  of  the  solution.  Suitable 
piping  with  simple  cocks  was  provided  for 
this  purpose.  Observations  of  the  rate  of  flow 
of  the  solution  were  made  by  the  aid  of  a 
meter.  A  glass  tube  forming  part  of  the  pip 
ing  system  made  visible  the  flow  of  the  chemi 
cal  solution. 

The  operation  of  filtering  the  partially  puri 
fied  (settled)  water  by  the  gravity  and  pres 
sure  filters,  and  the  manner  of  washing  these 
filters,  is  next  presented.  The  modification 
in  the  former  filter  in  April  makes  it  advisable 
to  consider  it  as  two  separate  filters,  gravity 
filters  (A)  and  (B). 

Operation  of  the  Western  Gravity  Filter  (A). 

The  water  from  the  settling  chamber  flowed 
through  a  4-inch  pipe  into  the  open  circum 
ferential  gutter  in  the  compartment  above  the 
sand,  from  which  it  overflowed  on  top  of  the 
sand  layer.  The  flow  through  this  pipe  was 
controlled  by  a  4-inch  gate  valve  operated  by 
hand,  and  a  4-inch  plug  operated  by  a  float 
in  the  open  compartment -referred  to  above. 

Filtration. — Starting  with  a  clean  sand  layer 
just  after  washing,  and  all  valves  closed,  the 
operation  of  filtration  was  proceeded  with  as 
follows: 


MANNER   OF  OPERATION  OF    THE  PURIFICATION  SYSTEMS. 


103 


The  gate  valve  on  the  inlet  from  the  set 
tling  chamber  to  the  filter  was  opened  and  the 
filter  allowed  to  fill  slowly  to  the  desired 
height.  As  a  usual  rule,  filtration  was  begun 
when  the  open  compartment  above  the  sand 
was  half  to  three-qarters  full,  and  it  was  then 
allowed  to  fill  till  the  flow  was  stopped  by 
the  plug  operated  by  the  float.  This  plug 
was  intended  to  regulate  the  rate  of  flow  of 
the  water  applied  to  the  filter. 

The  valve  on  the  filtered  waste-w'ater  pipe 
was  next  opened  and  the  water  allowed  to 
pass  downward  by  gravity  through  the  sand. 
Filtration  was  usually  begun  at  about  half  of 
the  normal  rate  or  less.  This  rate  was  held 
fairly  constant,  the  regulation  being  by  hand 
adjustment  of  the  valve,  until  the  water  began 
to  appear  clear.  The  rate  of  filtration  was 
then  slowly  increased  to  the  normal.  As  soon 
as  the  water  became  clear  at  the  normal  rate 
of  flow,  the  valve  on  the  waste-water  pipe  was 
closed  and  the  valve  on  the  main  outlet  pipe 
opened. 

Filtration  was  continued,  the  valve  on  the 
main  outlet  pipe  being  regulated  by  hand 
from  time  to  time  to  maintain  the  desired  rate, 
till  it  became  necessary  or  desirable  to 
wash. 

Decision  to  Wash  the  Filter. — It  may  be 
stated  that  the  cause  of  washing  this  filter  was 
in  practically  all  cases  the  exhaustion  of  the 
full  available  head  for  filtration.  When  the 
accumulations  on  and  in  the  sand  caused  a 
resistance  so  great  that,  with  the  outlet  valve 
wide  open,  the  rate  of  filtration  fell  below  that 
which,  in  the  opinion  of  the  operator,  it  was 
economical  or  desirable  to  maintain,  the  filter 
was  washed. 

Preparation  for  Wasliing  the  Filter. — When 
it  was  decided  to  wash  the  filter,  the  valve 
on  the  pipe  from  the  settling  chamber  to  the 
filter  was  closed,  and  the  water  above  the  sand 
was  allowed  to  filter  out.  This  was,  of  course, 
done  at  a  constantly  decreasing  rate,  owing 
to  the  increasing  resistance  and  the  decreas 
ing  head.  The  time  occupied  in  this  operation 
was  often  comparatively  long,  as  high  as  i 
hour  and  40  minutes  being  recorded,  while 
intervals  of  from  I  to  1.5  hours  were  quite 
common.  The  variations  in  the  quantity  of 
unfiltered  waste  water  (water  remaining  upon 
the  sand  after  draining  prior  to  washing)  are 


interesting  in  this  connection  and  will  be  pre 
sented  in  tables  in  Chapter  VIII. 

After  having  drained  through  the  sand 
layer  as  long  as  seemed  desirable,  the  re 
mainder  of  the  water  above  the  sand  was 
drawn  through  the  circumferential  gutter  and 
pipe  which  led  from  it  to  the  sewer. 

Washing  the  Filter. — The  operation  of 
washing  this  filter  consisted  in  opening  the 
valve  on  the  wash-water  pipe  to  its  full  extent 
and  letting  the  water  under  pressure  into  the 
strainer  system  beneath  the  sand.  From  the 
strainer  system  it  forced  its  way  up  through 
the  sand,  stirring  it  more  or  less  by  the  cur 
rent  of  the  water.  This  was  continued  till  the 
sand  was  sufficiently  cleansed  in  the  judgment 
of  the  operator,  when  the  wash-water  was 
shut  off.  The  maximum,  minimum,  and  aver 
age  vertical  velocities  of  the  wash-water  used 
with  this  filter  (estimating  45  per  cent,  of  the 
sand  layer  as  occupied  by  water)  were  3.42, 
1.22,  and  2.22  linear  feet  per  minute,  respec 
tively.  The  filter  was  then  ready  for  filling 
with  water  from  the  settling  chamber  prepara 
tory  to  filtration,  as  has  been  described. 

Operation  of  the  Western  Gravity  Filter  (B). 

Filtration. — This  operation  was  similar  to 
that  followed  in  Western  gravity  filter  (A), 
as  the  methods  of  regulating  the  flow  into 
the  filter,  starting  filtration  and  the  regulation 
of  the  rate  of  filtration  were  all  the  same  as 
in  the  original  filter. 

In  this  filter,  however,  washing  was  often 
found  advisable  before  the  available  head  was 
used  up. 

Decision  to  Wash  the  Filter. — This  question 
was,  as  with  the  other  systems,  a  matter  of 
judgment  with  the  operator.  Either  the  un 
satisfactory  appearance  of  the  effluent  or  "the 
decrease  in  rate  of  filtration  on  account  of  re 
sistance  of  the  filter  were  used  as  immediate 
guides  for  the  determination  of  the  time  of 
washing.  The  general  features  of  operation, 
character  of  river  water,  amount  and  charac 
ter  of  water  filtered,  and  several  other  allied 
factors,  however,  were  all  considered,  as  a 
rule. 

Preparation  for  Washing  the  Filter. — The 
manner  of  preparing  to  wash  the  filter 
was  practically  the  same  as  in  the  original 


I04 


WATER  PURIFICATION  AT  LOUISVILLE. 


filter.  Owing  to  the  small  column  of  water 
(only  about  3  feet)  maintained  above  the  sand, 
there  was  but  little  to  drain  out,  and  the  op 
eration  was  performed  quite  rapidly,  eight 
minutes  being  the  longest  time  recorded.  As 
a  rule,  however,  no  attempt  was  made  to  drain 
the  filter,  the  water  above  the  sand  being 
drawn  off  through  the  gutter  and  drain-pipe 
to  the  sewer,  as  far  down  as  the  top  of  the  col 
lecting  gutter.  The  filter  was  then  ready  for 
washing. 

Washing  the  Filter. — As  soon  as  the  filter 
was  drained,  the  valve  controlling  the  supply 
of  wash-water  was  opened,  and  the  water  ad 
mitted  freely  into  the  ball-nozzle  washing 
system.  The  water  was  allowed  to  pass  up 
through  the  sand  under  full  pressure,  until 
the  sand  was  considered  to  be  cleansed  to  the 
desired  degree.  The  wash-water  was  then 
shut  off  from  the  ball-nozzle  system,  and 
turned  into  the  strainer  system  for  a  period 
of  about  one  minute.  The  valve  on  the  wash- 
water  pipe  was  then  closed,  and  the  filter  was 
ready  for  filling  with  water  from  the  settling 
chamber  preparatory  to  filtration,  as  has  been 
described. 

In  washing  this  filter  an  average  vertical 
velocity  of  the  wash-water  (estimating  45  per 
cent,  of  the  sand  layer  as  occupied  by  water) 
of  2.25  linear  feet  per  minute  was  maintained, 
and  the  range  was  from  1.64  to  2.81  linear 
feet  per  minute. 

Operation  of  the  Western  Pressure  Filter. 

The  supply  for  this  filter  was  taken  from  the 
settling  chamber  through  a  6-inch  pipe,  and 
admitted  to  the  filter  under  full  pressure 
(about  45  pounds  to  65  pounds).  The  flow 
through  this  pipe  was  cut  off  when  desired 
by  a  valve  operated  by  hand. 

Filtration. — Starting  with  a  clean  sand 
layer  just  after  washing,  and  with  all  valves 
closed,  the  operation  was  as  follows: 

Water  from  the  settling  chamber  was  ad 
mitted  to  the  filter  through  the  inlet  pipe. 
The  valve  on  this  pipe  was  opened  wide  by 
hand.  As  the  pressure  filter  in  reality  was 
only  one  of  several  closed  compartments 
through  which  the  water  passed,  there  was 
no  filling  or  draining  the  tank  such  as  took 
place  in  the  gravity  filters. 


As  soon  as  the  valve  on  the  inlet  water- 
pipe  was  open,  the  valve  on  the  waste-water 
pipe  was  opened,  and  filtration  begun.  The 
most  distinctive  point  in  the  operation  of  this 
filter  was  the  pressure.  As  noted  above,  full 
pressure  was  carried  in  the  water  above  the 
sand,  and  the  valve  on  the  outlet  pipe  was 
opened  only  enough  to  cause  a  difference  in 
pressure  sufficient  to  allow  the  desired  amount 
of  water  to  pass  through  the  filter.  The 
available  head  in  this  filter  was  approximately 
1 1 5  feet  for  the  ordinary  minimum  pres 
sure. 

In  starting  filtration  it  was  always  cus 
tomary  to  waste  the  effluent  for  a  short 
period.  As  in  the  operation  of  the  Western 
gravity  filter,  the  rate  of  wasting  was  usu 
ally  about  half  of  the  normal  rate  until  the 
water  began  to  be  clear.  The  rate  was  then 
increased  up  to  the  desired  quantity;  the 
valve  on  the  waste-water  pipe  was  closed;  and 
the  valve  on  the  outlet  pipe  was  opened. 

Filtration  was  continued  until  it  was  found 
necessary  or  desirable  to  wash  the  filter.  The 
rate  of  filtration  was  regulated  from  time  to 
time  by  hand  adjustment  of  the  valve  on  the 
outlet  pipe. 

Decision  to  Wash  the  Filter. — In  this  filter 
two  factors  were  principally  used  as  guides 
to  determine  when  to  wash  it.  The  one  most 
often  relied  upon  was  the  appearance  of  the 
filtered  water.  The  other,  which  was  used 
mainly  during  the  early  part  of  the  test,  was 
the  loss  of  head  due  to  the  resistance  of  the 
sand  layer.  As  has  been  explained,  the  mini 
mum  available  head  was  about  1 15  feet.  This 
was  never  used  entirely,  however,  as  it  was 
deemed  advisable  to  wash  the  filter  when  the 
loss  reached  about  50  feet.  «In  some  cases 
when  the  appearance  of  the  filtered  water  was 
unsatisfactory  it  was  found  that  by  reducing 
the  rate  of  flow  for  a  short  time  the  water 
would  again  become  clear.  Under  these  con 
ditions  it  was  customary  to  waste  at  a  low  rate 
until  the  appearance  of  the  water  was  again 
satisfactory,  when  filtration  was  resumed. 

Preparation  for  Washing  the  Filter. — The 
preparation  for  washing  was  to  close  the 
valve  on  the  main  outlet  pipe  or  waste-water 
pipe  (whichever  was  in  use),  close  the  valve 
on  the  pipe  leading  from  the  settling  chamber 
to  the  filter,  and  then  open  the  valve  on  the 


MANNER   OF  OPERATION   OF   THE  PURIFICATION  SYSTEMS. 


branch  which  led  from  the  inlet  pipe  to  the 
sewer. 

Washing  the  Filter.  —  The  operation  of 
washing  the  filter  consisted  of  turning  the 
wash-water  under  full  pressure  into  the 
strainer  system  beneath  the  sand.  The  pres 
sure  of  the  water  forced  it  up  through  the 
sand  layer,  from  which  it  passed  out  through 
the  inlet  pipe  and  its  branch  to  the  sewer. 
Washing  was  continued  until  the  operator, 
judging  from  the  appearance  of  the  water  dis 
charging  into  the  sewer,  thought  the  sand 
was  cleansed  sufficiently.  The  valve  on  the 
wash-water  pipe  was  then  closed,  shutting  off 
the -supply  of  wash-water.  The  valve  on  the 
sewer  pipe  was  next  closed  and  the  filter  was 
at  once  ready  for  use. 

On  account  of  the  curved  sides  of  the  filter 
chamber  the  velocity  of  the  wash-water  varied 
at  different  points  in  the  sand  layer.  The 
maximum,  minimum,  and  average  vertical 
velocities  in  linear  feet  per  minute  were  as 
follows:  At  strainer  floor,  maximum  4.48, 
minimum  1.40,  average  2.68;  at  maximum 
horizontal  section  of  sand  layer,  maximum 
4.52,  minimum  1.23,  average  2.33;  at  sand 
surface,  maximum  5.68,  minimum  1.54,  aver 
age  2.93. 

It  will  be  seen  that  no  automatic  devices 
were  employed  in  connection  with  the  West 
ern  Pressure  System. 

Filtered  water  was  used  for  washing  the 
filter  during  the  major  portion  of  the  tests, 
but  during  the  period  from  June  24  to  July 
27  unfiltered  river  water,  admitted  at  the  full 
pressure  in  the  main,  was  used  for  this  pur 
pose. 

THE  MECHANICAL  DEVICES  INSTALLED  AND 
USED  TO  AID  IN  THE  OPERATION  OF  THE 
RESPECTIVE  SYSTEMS. 

Under  this  section  the  special  devices  used 
by  the  several  systems  will  be  described  in  the 
following  order: 

Devices  to  regulate  the  admission  of  river 
water  to  the  systems. 

Devices  to  regulate  the  flow  of  water  from 
the  settling  basins  or  chambers  to  the  filters. 

Devices  to  regulate  the  admission  of  chemi 
cal  solution. 

Devices  to  regulate  the  rate  of  filtration. 


Devices  Used  to  Regulate  the  Admission  of 
River  Water. 

Warren  System. — The  flow  of  river  water 
under  pressure  into  the  settling  basin  was 
regulated  by  a  5-inch  valve  operated  by  hand, 
and  a  common  6-inch  balanced  valve  operated 
by  a  float  in  the  settling  basin.  The  float  was 
a  cylinder  fixed  on  the  end  of  an  arm  fastened 
to  the  side  of  the  basin.  The  arm  was  ap 
proximately  3  feet  long.  About  0.75  foot 
from  the  fixed  end  of  the  arm  a  chain  con 
nected  to  the  valve  stem.  The  relative  motion 
of  the  float  and  valve  was  therefore  about  4 
to  i. 

Jewell  System. — The  flow  of  river  water 
under  pressure  into  the  settling  chamber  was 
regulated  by  a  5-inch  valve  operated  by  hand 
and  a  5-inch  single-seated  valve  operated  by 
a  float  in  the  open  compartment  of  the  filter 
above  the  sand.  The  float  was  a  metal  cylin 
der  attached  to  an  arm  3.67  feet  long,  one  end 
of  which  was  fastened  to  the  beam  supporting 
the  agitator  machinery.  From  the  other  end 
of  the  cylinder  extended  an  arm  to  which  was 
attached  a  chain  leading  down  through  a 
small  vertical  pipe  to  the  valve  mechanism  on 
the  inlet  water-pipe.  The  total  length  from 
the  fixed  end  of  the  float  to  the  point  where 
the  chain  was  fastened  was  5.17  feet.  The 
chain  was  fastened  on  the  long  arm  of  a  bell- 
crank  lever,  the  arms  of  which  were  i  .84  feet 
and  0.21  foot  long,  respectively.  The  short 
end  was  fastened  by  a  wrist-pin  to  an  arm  o.  18 
foot  long,  which  in  turn  connected  with  the 
valve  plate  by  means  of  a  wrist-pin.  The 
valve  plate  was  connected  with  a  fixed  arm 
hinged  on  one  side  of  the  frame.  The  dis 
tance  from  the  wrist-pin  on  the  valve  plate  to 
the  hinge  about  which  the  valve  moved  was 
0.33  feet.  This  combination  of  levers  caused 
a  motion  of  the  valve,  the  relation  of  the 
movement  to  that  of  the  float  depending  upon 
the  position  of  the  float.  When  the  latter  was 
down,  the  valve  was  given  its  greatest  pro 
portional  movement.  When  the  float  ap 
proached  its  highest  position,  the  short  arm  of 
the  bell-crank  and  the  arm  attached  to  the 
valve  approached  a  straight  line,  and  the 
movement  of  the  valve  became  very  small. 

Western  Systems. — The  supply  for  these 
systems  was  regulated  only  by  controlling 


io6 


WATER  PURIFICATION  AT  LOUISVILLE. 


the  rate  of  flow  to  the  filters  as  described  be 
yond.  The  main  water  pump  aided  somewhat 
in  maintaining  a  uniform  pressure  of  the 
water,  but  cannot  be  said  to  have  been  used 
as  a  device  for  regulating  the  flow  of  water. 

Devices  Used  to  Regulate  the  Flow  of  Water 

from  the  Settling  Chambers  to  the 

Respective  Filters. 

Only  one  special  device  can  be  said  to  have 
been  used  directly  for  this  purpose,  viz.,  the 
plug  operated  by  a  float  in  the  Western 
gravity  filter.  In  operation,  however,  the 
device  used  by  the  Jewell  System  for  regulat 
ing  the  admission  of  water  to  the  settling 
chamber  acted  as  a  controlling  device  in  this 
connection,  as  did  also  the  similar  mechanism 
in  the  Warren  System. 

Devices  Used  to  Control  the  Application  of  Alum 
or  Sulphate  of  Alumina. 

Warren  System. — The  sulphate  of  alumina 
solution  admitted  to  the  pump  box  was  regu 
lated  by  a  valve  operated  by  a  float  in  the 
pump  box.  The  float  arm  was  vertical,  the 
relation  between  the  position  of  the  valve  and 
the  level  of  the  solution  being  adjustable  by 
changing  the  length  of  the  vertical  arm.  The 
rate  of  discharge  of  solution  by  the  pump  for 
each  revolution  was  capable  of  variation  by 
means  of  the  insertion  of  stoppers  in  the  ends 
of  the  pump  arms. 

This  operation  was,  of  course,  performed 
by  hand.  The  pump  itself  was  the  main  regu 
lating  device,  because  it  was  operated  by  the 
flow  of  the  water  in  the  main  inlet  water-pipe, 
and  its  rate  of  revolution  was  designed  to  be 
proportional  to  the  flow  of  water  through  the 
pipe. 

Jewell  System. — During  the  first  five 
months  of  the  test  the  movement  of  a  float 
at  the  top  of  the  filter,  as  described  above,  was 
relied  upon  to  regulate  the  rate  of  application 
of  the  solution  of  sulphate  of  alumina,  by  ad 
justing  the  throttle-valve  on  the  chemical 
pump.  After  this  was  abandoned,  hand  regu 
lation  alone  was  used. 

Western  Systems. — In  the  original  device 
used  by  these  systems  the  method  used  for 
regulating  the  application  of  alum  solution 


was  by  hand  adjustment  of  the  valve  on  the 
alum  pipe.  The  arrangement  of  the  device 
allowed  adjustment  by  regulating  the  differ 
ence  in  pressure  in  the  two  alum  pipes, 
which  was  done  by  changing  the  position  of 
the  valve  on  the  main  inlet  water-pipe.  This 
was  only  used  in  starting  operation,  how 
ever. 

In  the  second  Western  device  the  method 
of  adjusting  the  application  of  chemicals  was 
by  hand  regulation  of  the  return  or  relief  out 
let  valves. 

Devices  Used  for  Regulating  the  Rate  of 
Filtration. 

Warren  System. — The  regulating  device 
used  in  this  system  was  a  movable  weir.  This 
has  already  been  fully  described  in  Chapter 
V.  As  a  rule  it  was  adjusted  about  every 
half-hour.  A  valve  operated  by  hand  was 
used  for  regulating  the  rate  of  wasting. 

Jeivell  System. — As  described  in  section  I 
of  this  chapter,  the  rate  of  filtration  was  regu 
lated  by  means  of  hand  valves  up  to  April  10, 
1896.  On  this  date  a  device  called  an  "  auto 
matic  controller "  was  installed.  The  ar 
rangement  of  this  device  was  as  follows: 
SBA\  ,i3;iy  aqi  UIQJJ  adid  }3[}no  UIEUI  3t[j, 
raised  up  and  the  end  turned  down,  so  that  it 
discharged  into  a  galvanized  iron  tank  through 
a  4-inch  butterfly  valve.  Through  this  pipe 
the  flow  was  regulated  by  the  valve,  which  in 
turn  was  controlled  by  the  position  of  a  bal 
ance  arm  on  the  valve  stem.  The  iron  tank, 
i  foot  in  diameter,  was  hung  from  the  outlet 
pipe  by  four  arms.  Its  upper  end  was  open. 
The  outlet  from  this  tank  was  a  sharp-edged 
orifice  at  the  bottom,  through  which  the 
water  was  discharged  into  a  galvanized  iron 
funnel,  which  led  the  water  into  the  pipe  con 
nected  with  the  filtered-water  reservoir. 

The  regulation  of  the  flow  was  obtained  by 
the  butterfly  valve  above  mentioned,  the  posi 
tion  of  the  valve  been  controlled  by  the  level 
in  the  tank  in  the  following  manner: 

The  balance  arm  of  the  valve  held  an  iron 
weight  at  one  end  and  a  copper  cylinder  at  the 
other.  This  copper  cylinder  had  a  discharge 
port  and  funnel  at  the  bottom.  From  the 
bottom  of  the  iron  tank  a  flexible  pipe,  with 
an  overflow,  fed  into  the  small  copper  cylin- 


MANNER   OF  OPERATION  OF    THE  PURIFICATION  SYSTEMS. 


107 


der  above  mentioned,  and  the  water  in  the 
cylinder  flowed  back  into  the  funnel  on  the 
pipe  to  the  reservoir. 

The  small  overflow  pipe  was  adjustable  to 
any  desired  height  so  that  it  would  cause  the 
desired  rate  of  flow  through  the  orifice  in  the 
bottom  of  the  iron  tank.  The  parts  were  so 
proportioned  that  if  the  water  remained  con 
stantly  at  the  desired  level,  the  overflow  into 
the  small  cylinder  was  just  sufficient  to  keep 
the  water  in  this  cylinder  at  a  height  neces 
sary  to  balance  the  weight  on  the  other  end 
of  the  lever  arm,  thus  keeping  the  valve  open 
the  required  amount.  When  the  flow  in 
creased  or  decreased,  the  overflow  became 
greater  or  smaller,  and  the  level  of  the  water 
in  the  small  cylinder  therefore  increased  or 
decreased.  The  balance  arm  moved  corre 
spondingly,  thus  closing  or  opening  the  valve. 

Western  System. — Hand  valves  alone  were 
used  for  regulating  the  rate  of  filtration  in  the 
Western  Systems. 

THE  ATTENTION  GIVEN  TO  THE  RESPECTIVE 
SYSTEMS. 

The  general  manner  of  operation  of  the 
respective  systems,  and  the  special  devices  in 
stalled  to  aid  the  operators,  have  already  been 
presented.  In  this  section,  the  number  of 
men  which  the  several  companies  considered 
necessary  to  employ  to  operate  the  respective 
systems  will  be  given.  It  is  not  the  pur 
pose  of  this  section  to  present  any  compara 
tive  statements  for  the  purpose  of  showing 
the  number  of  men  necessary  to  operate  any 
modification  or  enlargement  of  these  systems, 
but  to  show  clearly  the  amount  and  character 
of  supervision  deemed  necessary  by  the  dif 
ferent  filter  companies  for  the  operation  of 
their  respective  systems. 

From  March  24  to  29,  inclusive,  the  sys 
tems  were  operated  day  and  night.  For  six 
weeks  beginning  April  27  the  systems  were 
operated  continuously  from  9  A.M.  on  Mon 
day  to  4  P.M.  on  Saturdays  of  each  week. 


The  Number  of  Men  Engaged  in  the  Operation 
of  the  Respective  Systems. 

Warren  System. — Throughout  the  test  this 
system  was  in  charge  of  a  trained  engineer 
who  was  also  a  chemist.  He  was  assisted  by 
one  regular  helper.  During  the  continuous 
run  in  March,  the  system  was  operated  at 
night  by  a  superintendent  of  the  company. 
During  the  six  weeks'  run  the  regular  assist 
ant  took  charge  at  night,  and  a  second  helper 
was  employed  during  the  day. 

Jewell  System. — From  the  beginning  of  the 
test  till  Nov.  n,  1895,  the  system  was  oper 
ated  by  one  man  who  was  a  chemist.  After 
Nov.  1 1  an  officer  of  the  company  was  in 
charge.  He  was  assisted  till  Nov.  18  by  the 
original  man  in  charge.  On  that  date  an 
other  chemist  was  employed  in  place  of  the 
original  chemist.  This  chemist  was  replaced 
during  the  second  week  in  December  by  a 
mechanic.  A  boy  was  employed  after  the  first 
week  in  December.  This  force  of  two  men 
and  a  boy  remained  up  to  March  23,  when  a 
chemist  was  employed.  No  change  was  made 
in  this  force  of  three  men  and  a  boy  through 
out  the  balance  of  the  test  except  during  the 
continuous  run  in  March. 

During  this  continuous  run  the  system  was 
operated  during  the  day  by  an  officer  of  the 
company  assisted  by  the  chemist,  and  during 
the  night  by  another  officer  assisted  by  the 
mechanic  and  the  boy.  During  the  six  weeks' 
continuous  run  the  force  of  three  men  was 
divided  into  three  watches,  the  boy  assisting 
about  the  place  during  the  day. 

Western  Systems. — These  systems  were  in 
charge  of  a  trained  chemist  throughout  the 
test.  He  was  assisted  in  the  routine  operation 
by  one  and  sometimes  two  men.  Up  to 
March  24  only  one  helper  was  employed.  A 
new  man  was  employed  to  assist  during  the 
day  at  the  beginning  of  the  first  continuous 
run,  the  original  helper  being  on  duty  at 
night.  Two  men  were  employed  from  this 
time  till  the  first  week  in  July.  A  boy  was 
also  employed  to  assist  at  night  throughout 
the  six  weeks'  continuous  run. 

The  influence  on  the  results  accomplished 
by  the  systems  of  the  attention  received  will 
be  considered  further  in  Chapter  IX. 


io8 


WATER   PURIFICATION  AT  LOUISVILLE, 


CHAPTER  VIII. 

COMPOSITION  OF  THE  OHIO  RIVER  WATER  AFTER  TREATMENT  BY  THE  RESPECTIVE 
SYSTEMS  OF  PURIFICATION,  AS  SHOWN  BY  CHEMICAL,  MICROSCOPICAL,  AND  BAC 
TERIAL  ANALYSES;  TOGETHER  WITH  A  TABULATION  OF  THE  MOST  IMPORTANT  DATA 
ON  THE  OPERATION  OF  THE  RESPECTIVE  SYSTEMS. 


IN  this  chapter  is  recorded  the  main  bulk 
of  the  detailed  results  of  the  observations  and 
examinations  made  during  the  investigations. 
These  results  are  presented  in  a  series  of 
tables  as  follows: 

Table  No.  I,  results  of  regular  chemical 
analyses,  indicating  the  sanitary  and  technical 
characters  of  the  water  after  purification. 

Table  No.  2,  results  of  mineral  analyses  of 
the  water  after  purification. 

Table  No.  3,  results  of  microscopical  ex 
aminations  of  the  water  after  purification. 

Table  No.  4,  results  of  bacterial  analyses  of 
the  water  after  purification,  and  a  record  of 
conditions  under  which  each  sample  was  col 
lected. 

Table  No.  5,  records  of  the  operation  of  the 
respective  systems,  including  a  brief  summary 
of  the  analytical  results  and  also  the  amount 
of  sulphate  of  alumina  used  during  each  run. 

The  next  chapter,  in  which  these  results  are 
summarized  and  discussed,  also  contains  some 
analytical  and  other  results  which  were  ob 
tained  in  connection  with  special  points  which 
are  outlined  in  the  discussion.  This  chapter 
deals  solely  with  the  principal  detailed  rec 
ords.  In  the  case  of  each  table  there  are  a 
number  of  explanations  and  points  to  which 
attention  is  called,  as  stated  in  the  following 
paragraphs.  It  may  again  be  stated  that 
effluent  refers  to  the  water,  after  its  passage 
through  one  of  the  systems,  which  was  passed 
into  the  outlet  provided  for  the  finished  prod 
uct.  It  is  further  to  be  noted  that  whenever 
filtration  or  any  related  term  is  used,  it  refers 
to  effective  filtration,  i.e.,  the  filtration  of 
water  which  was  passed  into  the  outlet  pro 
vided  for  the  finished  effluent. 


Table  No.  i. 

Samples. — The  samples  of  the  several 
effluents,  for  regular  chemical  analysis,  are 
listed  in  serial  numbers.  The  same  series  of 
numbers  was  used  for  both  the  untreated  river 
water  and  the  effluents.  During  the  process 
of  analysis  samples  were  designated  by  these 
numbers  only,  and  the  source  of  the  samples 
was  not  known  to  the  analysts.  The  condi 
tions  under  which  the  samples  were  collected 
are  presented  as  a  matter  of  convenience  by 
reference  to  Table  No.  5,  which  includes  the 
results  of  bacterial  analyses  of  corresponding 
samples.  During  a  portion  of  the  time 
samples  for  chemical  analysis  were  collected 
continuously  by  an  automatic  device  which  is 
briefly  described  in  the  appendix.  In  such 
cases  the  period  covered  by  the  sample  is  re 
corded. 

In  cases  where  several  portions  of  effluent 
were  mixed  together  for  a  single  average 
sample,  the  water  was  kept  in  an  ice-box  dur 
ing  the  period  which  intervened  between  the 
times  of  collection  and  of  analysis. 

Methods  of  Analysis. — Substantially  the 
same  methods  were  employed  for  the  analysis 
of  effluents  as  were  used  in  the  case  of  the 
untreated  river  water.  They  are  presented 
briefly  in  Chapter  I.  The  only  point  to  be 
mentioned  is  that  in  the  present  tabulations 
there  are  included  results  indicating  the  ap 
pearance  of  the  effluents.  These  results  are 
given  under  the  heading.  "  Degree  of  Clear 
ness."  They  were  obtained  by  careful  inspec 
tion,  aided  by  a  diaphanometer  such  as  is 
briefly  described  in  the  appendix,  where  an 
outline  of  the  methods  followed  will  be  found. 


COMPOSITION  OF  OHIO   RIVER    WATER   AFTER  PURIFICATION. 


109 


The  significance  of  the  five  degrees  of  clear 
ness  is  substantially  as  follows: 

Degree  No.  i,  brilliant. 

Degree  No.  2,  clear. 

Degree  No.  3,  slightly  turbid. 

Degree  No.  4,  turbid. 

Degree  No.  5,  very  turbid. 

These  expressions  relate  to  perfectly  clear 
water  as  a  basis  of  comparison,  and  have 
nothing  to  do  with  such  expressions  as  might 
be  applied  to  the  muddy  river  water.  No  ob 
jection  could  be  raised  by  consumers  with  re 
gard  to  the  appearance  of  the  effluents  when 
it  was  represented  by  any  of  the  first  three 
degrees  of  clearness;  with  the  fourth,  the 
turbidity  would  probably  be  noticed  by  con 
sumers  at  times,  but  not  uniformly. 

Color. — The  color  of  the  effluents,  so  far  as 
related  to  dissolved  matters  in  the  water,  was 
very  slight,  as  is  also  true  of  the  Ohio  River 
water  before  treatment.  Some  of  the  color  re 
sults  were  unavoidably  increased  by  minute 
particles  suspended  in  the  water. 

Carbonaceous  Organic  Matter — Oxygen  Con 
sumed. — The  carbonaceous  organic  matter  in 
the  effluents,  as  indicated  by  the  oxygen  con 
sumed,  was  satisfactory,  practically  without 
exception,  and  was  less  than  that  dissolved  in 
the  river  water. 

Nitrogenous  Organic  flatter — Albuminoid 
Ammonia. — The  nitrogenous  organic  matter 
in  the  effluents,  as  indicated  by  the  nitrogen 
in  the  form  of  albuminoid  ammonia,  was  also 
satisfactory  as  a  rule,  and  less  than  that  dis 
solved  in  the  river  water.  Very  little  or  no 
organic  matter  was  suspended  in  the  effluents 
ordinarily.  In  effluents  which  had  either  of 
the  first  two  degrees  of  clearness  it  is  recorded 
as  zero.  In  the  other  three  degrees  of  clear 
ness  it  was  appreciable;  but  it  was  too  small 
for  measurement  in  a  satisfactory  manner, 
and  accordingly  blanks  are  inserted  in  the 
tables  under  these  conditions. 

Nitrogen  as  Free  Ammonia  and  Nitrites. — As 
a  rule  there  was  a  slight  reduction  in  the 
effluents,  as  compared  with  the  river  water, 
in  these  compounds,  which  represent  inter 
mediate  steps  in  the  conversion  of  organic 
matter  in  its  crude  form  into  completely 
oxidized  mineral  matter. 

Nitrogen  as  Nitrates. — There  was  sub 
stantially  no  change  in  the  water  before  and 


after  treatment  with  regard  to  the  amount  of 
nitrogen  in  the  form  of  nitrates.  This  deter 
mination  indicates  the  amount  of  organic 
matter  which  is  completely  oxidized  ;  and 
it  is  not  to  be  expected  that  the  amounts 
would  change  after  treatment  of  the  water  by 
a  process  in  which  the  organic  matter  is  re 
moved  mechanically — not  by  oxidation  and 
nitrification. 

Chlorine. — The  chlorine  in  the  water  was 
not  affected  by  the  treatment. 

Residue  on  Evaporation. — The  suspended 
matter  in  the  river  water  was  completely  re 
moved  in  a  majority  of  cases  by  the  treat 
ment,  as  well  as  some  of  the  dissolved  mat 
ters.  Whenever  the  effluents  had  a  degree 
of  clearness  of  No.  4  or  No.  5,  there  was  an 
appreciable  amount  of  mineral  matter  sus 
pended  in  it,  but  it  could  not  be  satisfactorily 
measured. 

I'i.rcd  Residue  on  Evaporation. — These  re 
sults  are  given  as  a  matter  of  record  for  com 
parison  with  corresponding  results  of  the 
water  before  treatment. 

Alkalinity. — The  alkalinity  of  the  effluents, 
caused  chiefly  by  lime  (carbonate  and  bicar 
bonate  of  calcium),  was  less  than  that  of  the 
river  water  by  a  quantity  almost  directly  pro 
portional  to  the  amount  of  sulphate  of  alu 
mina  used  in  the  treatment  of  the  water.  In 
some  instances  the  alkalinity  was  exhausted, 
due  to  an  excess  of  sulphate  of  alumina,  and 
the  effluents  were  acid. 

Dissolved  Alumina. — As  a  rule  the  analyses 
indicated  the  effluents  to  be  completely  free 
from  dissolved  alumina,  although  at  times 
mere  traces  were  noted  in  the  course  of  anal 
ysis. 

The  question  of  alkalinity  and  dissolved 
alumina  have  already  received  careful  consid 
eration  in  Chapter  III. 

Iron. — With  the  possible  exception  of  very 
slight  traces  of  dissolved  iron,  all  of  the  iron 
in  the  river  water  was  removed  except  when 
the  effluents  were  quite  turbid.  In  many  cases 
it  appeared  that  iron  was  contained  in  the  par 
ticles  which  made  the  effluents  turbid. 

Table  No.  2. 

In  this  table  are  recorded  the  results  of 
mineral  analyses  of  the  several  effluents  dur- 


WATER   PURIFICATION  AT  LOUISVILLE. 


ing  the  period  of  continuous  operation,  from 
March  23  to  29,  inclusive.  During  this  time 
samples  of  the  effluents  were  collected  con 
tinuously  by  automatic  devices.  As  a  matter 
of  convenience  for  comparison,  the  mineral 
analyses  of  the  corresponding  river  samples 
are  also  presented. 

These  results  are  of  value  in  showing  the 
constituents  which  composed  the  mineral 
matter  in  the  water  before  and  after  treat 
ment. 

Table  No.  3. 

This  table  contains  the  results  of  micro 
scopical  analyses  of  the  effluents  for  algae, 
diatoms  and  such  micro-organisms  as  may  be 
enumerated  and  classified  with  the  aid  of  the 
microscope,  and  without  the  aid  of  special 
methods  such  as  are  necessary  in  the  case  of 
the  bacteria. 

Practically  speaking,  the  effluents  were  free 
from  this  class  of  living  organisms. 

Table  No.  4. 

The  results  of  the  determinations  of  the 
numbers  of  bacteria  in  the  effluents  are  re 
corded  in  this  table.  The  samples  were 
given  a  number  in  the  series  which  included 
also  the  samples  of  river  water.  In  addition 
to  the  hour  of  collection  of  the  sample  a  rec 
ord  is  also  given  of  the  "  run  "  during  which 
the  collection  was  made.  This  facilitates  a 
detailed  study  of  the  entire  records,  including 
those  of  the  following  table.  A  run  was  re 
garded  during  these  investigations  as  com 
prising  all  the  normal  operations  of  the 
respective  systems,  from  the  first  opening  of 
the  valve  on  the  filtered-water  pipe,  following 
a  wash,  to  the  next  succeeding  similar  opera 
tion. 

The  rate  of  filtration,  expressed  in  cubic 
feet  per  minute  and  million  gallons  per  acre 
per  24  hours,  and  the  loss  of  head  at  the  time 
of  collection  of  the  samples  are  also  presented. 
It  will  be  noted  that  the  loss-of-head  observa 
tions  were  not  made  at  the  outset  of  the  inves 
tigations.  This  was  caused  by  unavoidable 
delays  in  providing  proper  facilities  for  ob 
taining  full  sets  of  observations.  The  period 
of  time  occupied  in  filtration,  and  the  quan 
tity  of  water  filtered,  between  the  resumption 


of  filtration  following  the  preceding  washing 
of  the  sand  layer  and  the  collection  of  the 
samples,  are  each  recorded.  Under  the  re 
marks  will  be  found  comments  upon  special 
features  in  the  operation  of  the  respective 
systems  in  association  with  the  sample  ana 
lyzed.  A  series  of  letters  will  also  be  noted 
under  the  column  of  remarks.  They  serve  as 
a  guide  in  showing  the  basis  upon  which  the 
average  bacterial  efficiencies  of  the  respective 
systems  were  computed,  as  follows: 

A.  Those  abnormal  results  which  were  ob 
tained  at  the  extreme  end  of  a  run  just  prior 
to  washing,  and  which  are  not  included  in 
averages. 

B.  The  results  of  special  samples  collected 
in  special  places,  and  of  those  taken  after  the 
system  had  been  out  of  operation  for  periods 
of  greater  or   less   duration,   both   of  which 
were  therefore  not  included  in  averages. 

C.  When    two    sets    of    bacterial    samples 
were  collected,  one  set  taken  "  all  at  once  " 
and    the    other    collected    by    an    automatic 
sampler  and  covering  a  long  period,  only  one 
set  of  results  were  used  for  official  averages. 
Those  results  designated  by  the  letter  C  were 
used  only  as  checks. 

D.  Those    results    were    excluded    which 
were  obtained  at  times  when  the  operations 
were  under  conditions  known  to  be  abnormal, 
and    which    were    in    the    majority    of    cases 
caused  by  the  Water  Company. 

E.  Long  series  of  results  on  certain  runs, 
when   the   automatic   samplers   were   in   use, 
were  excluded  from  the  daily  averages,  but 
were  used  exclusively  in  obtaining  the  aver 
ages  for  those  particular  runs. 

Table  No.  5. 

This  table  contains  the  records  of  the 
operation  of  the  respective  systems  tabulated 
in  the  form  of  runs.  As  stated  above,  all 
normal  operations  of  the  respective  systems 
from  the  first  opening  of  the  valve  on  the  fil 
tered-water  pipe  following  a  wash  to  the  next 
succeeding  similar  operation  composed  a  run, 
according  to  the  system  of  records  employed 
in  these  investigations.  The  several  head 
ings,  under  which  the  data  upon  each  indi 
vidual  run  are  grouped,  are  defined  as  fol 
lows: 


COMPOSITION  OF  OHIO  RIVER    WATER   AFTER  PURIFICATION. 


Period  of  Operation. — This  includes  all  the 
time  devoted  to  normal  operation  of  the  sys 
tem. 

Period  of  Service. — The  time  during  which 
water  passed  through  the  pipe  provided  for 
the  finished  product,  i.e.,  the  period  of  effec 
tive  filtration. 

Period  of  Wash.- — The  time  occupied  in 
preparing  the  filter  for  filtration,  comprising 
the  time  occupied  in  washing  the  sand  layer, 
filling  the  filter,  and  wasting  the  filtered 
water  when  considered  necessary. 

Period  of  Delay. — The  time  which  was  not 
used  in  normal  operation  of  the  system  from 
the  beginning  to  the  end  of  the  run. 

Quantities  of  Water. — These  are  all  ex 
pressed  in  cubic  feet  as  actually  recorded  by 
the  meters,  except  the  unfiltered  waste  water, 
which  was  determined  from  gauge  observa 
tions. 

Applied  Water. — The  total  quantity  of 
river  water  treated  by  the  system. 

Filtered  Water. — The  total  quantity  of  fil 
tered  water  turned  into  the  outlet  provided 
for  the  finished  product. 

Filtered  Waste-water. — The  total  quantity 
of  filtered  water  which  was  wasted. 

Unfiltered  Waste-water. — The  total  quantity 


of  unfiltered  water  which  was  removed  from 
above  the  sand  layer  prior  to  washing. 

The  remaining  headings  are  self-explana 
tory,  but  attention  may  be  called  to  the  sum 
maries  for  each  run  of  the  following  data, 
dealing  with  the  efficiency  and  economy  of 
purification: 

1.  The  amount  of  sulphate  of  alumina  ap 
plied  to  the  river  water  in  grains  per  gallon. 

2.  The    estimated    amount    of    suspended 
matter,    in    parts    per    million,    in    the    river 
water. 

3.  The    average    number    of    bacteria    per 
cubic  centimeter  in  the  river  water  and  in  the 
effluents. 

4.  The  maximum  and  minimum  number  of 
bacteria  per   cubic   centimeter  found   in  the 
effluents. 

5.  The  average  bacterial  efficiency,  which 
was    computed    by    taking    the    percentage 
which  the  difference  in  the  average  numbers 
of   bacteria   in    the    river   water   and    in    the 
effluent  was  of  the  average  number  of  bacteria 
in  the  river  water. 

Special  features  are  noted  under  "  Remarks." 
Those  runs  marked  with  a  star  (*)  were  made 
under  abnormal  conditions  and  are  excluded 
from  subsequent  averages  and  summaries. 


WATER   PURIFICATION  AT  LOUISVILLE. 


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COMPOSITION  OF  OHIO  RIVER    WATER  AFTER  PURIFICATION. 


127 


TABLE  No.  2. 

RESULTS   OF    MINERAL   ANALYSES   OF   THE   OHIO    RIVER   WATER    BEFORE    AND   AFTER 

PURIFICATION    BY    THE    RESPECTIVE    SYSTEMS. 

(Parts  per  Million.) 


ce  of  Sample. 


Silica (SiO.,) 

Oxide  of  iron .(Fc3Oj)   

Alumina (AljO,) 

Oxide  of  manganese (MnO) 

Oxide  of  nickel     (NiO)   

Lime (CaO) 

Magnesia (MgO) 

Soda (Na,O) 

Potash (K,O) 

Chlorine .  .  .(Cl) 

Nitric  acid (N,O5) 

Carbonic  acid,  combined (CO2) 

Sulphuric  acid (SO,) 

Phosphoric  acid (PjOs) 


Ri 


299 . 50 
39-45 
76.55 

2.  2O 
I  .09 

3' -/o 
13.98 

8.48 
18.15 

5-57 
14.67 
2I.2S 
23.28 

0.79 


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0.15 

2.05 
none 

less  than  I  .o 
30 . 60 

7-03 

5.02 

8.19 

5-54 
14.67 

7-75 
35-71 

0.98 


Jewell  Kffluent.          Western  I'res.  Eff. 

4   00 

o.  1 1 

0.24 
trace 

less  than  I 
33-22 

6.64 

3.56 

7.85 

5-78 
13.89 
13.12 
33-37 

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less  thi 
34 
6, 

8 


41. 


0.47 


TABLE  No.  3. 

RESULTS    OF   MICROSCOPICAL    ANALYSES    OF   THE    EFFLUENTS    OF   THE    RESPECTIVE   SYSTEMS 
(Number  of  Organisms  per  Cubic  Cemimeter.)* 


1896 
Feb.        18 


'9 

26 

March      4 


March     4 


April 
May 


June 


April 
May 


June 


July 


Feb. 
March 


May 

June 
uly 


Number  of 
Sample. 


Total   Number, 


Effluent  of  the  Warren  System. 

278          Diatomaceae:  Synedra,  8;  Chlorophyceae:  Protococcus,  2;  Infusoria: 
Parts  of  cases,  6 

281  Oiatomaceae:  Navicula  and  Cymbclla  pr 

305  No  organisms  present 

330  Diatomaceae.   Synedra,  pr;  Fungi:  Crenothrix,  pr 

355          Diatomaceae:   Synedra,  3 

383          Diatomaceae:  Meridion,  pr;  Miscellaneous:   Anguillula,  I 

405  Miscellaneous:  Anguillula,  pr 

460  No  organisms  present 

518          Chlorophyceae:   Protococcus,  I ;  Miscellaneous:  Vegetable  Hairs,  23 

545  Diatomaceae:    Synedra,    i;    Cymbella,    i;    Chlorophycene:     Proto 

coccus,  i 

567          Chlorophycete:   Protococcus,  pr;   Infusoria:  Trachelomonas,  pr.  . . 
588          Diatomaceas:  Synedra  and  Cyclotella,  pr 

630  Chlorophyceae:   Conferva,  pr 

652  Verities:   Ploima,  26;  Miscellaneous:  Zoospores,  16 

Effluent  of  Jewell  System. 

282  Diatomaceae:   Syr.edra,  Navicula,  pr 

306  .Diatomaceae:    Pleurosigma,    Cymbella,   pr;    Chlorophyceae:     Proto 

coccus,  Scenedesmus,  pr 

328         :No  organisms  present 

353         iNo  organisms  present 

381          iNo  organisms  present 

406  [Fungi:   Mould  hyphae,  pr 

461  i  No  organisms  present 

472          Chlorophyceae:   Protococcus,  pr 

517         |Chlorophyceae:   Protococcus,  16;  Miscellaneous:  Anguillula,  I  .... 

546  | Miscellaneous:  Zoospores,  pr   

566         jDiatomacese:  Synedra,  pr;    Chlorophyceae:    Prolococcus,  i;   Scene 
desmus,  2;  Miscellaneous:  Zoospores,  pr 

587          Diatomaceae:    Synedra,    pr;    Cyclotella,    i;    Chlorophyceae:    Proto 
coccus,  2;    Pandorina,  pr;   Endorina,  pr;  Vermes:   Plorima,  pr.. 

63 1  Chlorophyceae:    Protococcus,  pr 

653  No  organisms  present 

685          Infusoria:   Monas,  12;   Miscellaneous:  Zoospores,  pr 

709          No  organisms  present 

Effluent  of  Western  Gravity  System. 

307  No  organisms  present. . .    

331  No  organisms  present 

350          Chlorophyceae:  Spyrogyra, I 

380          Chlorophyceae:   Protococcus,  pr 

Effluent  of  Western  Pressure  System. 

308  No  organisms  present 

332  No  organisms  present 

350          No  organisms  present 

374          Chlorophyceae:   Piotococcus,  I 

407  No  organisms  present 

565          Chlorophyceae:   Protococcus,  5 

586          Diatomaceae:  Cyclotella,  pr 

654  No  organisms  present 

718         Chlorophyceae:  Protococcus.  pr . .._._ 

*pr  —  present. 


16 
pr. 

o 
pr. 

3 

i 
pr. 

o 
24 

3 
pr. 

pr. 
pr. 
42 


128 


WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  4. 

RESULTS   OF    BACTERIAL   ANALYSES   OF   THE    EFFLUENTS   OF   THE    RESPECTIVE   SYSTEMS. 

Warren   System. 


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I  825 

46 

64 

"      25 

4-34     ' 

4 

25.0 

137 

2h.  24m. 

32/4 

33 

66 

"      26 

10.56  A.M. 

4 

25.0 

137 

4h.  26m. 

7  205 

65 

69 

"      26 

1.  12    P.M. 

4 

24.0 

132 

6h.  42m. 

9493 

31 

71 

"      26 

4.40       " 

4 

20.0 

no 

loh.  lom. 

13  527 

32 

73 

"       28 

12.10       " 

5 

26.0 

M3 

45m. 

i  127 

61 

74 

"    28 

1.  10       " 

5 

26.0 

M3 

ih.  45m. 

2  671 

28 

75 

"       28 

2.30       " 

5 

23.0 

126 

3h.  05m. 

4554 

28 

76 

"    28 

3.23       " 

5 

25.0 

138 

3h.  s8m. 

5  802 

3° 

79 

"   29 

12.33       " 

6 

27.0 

148 

ih.  33m. 

2357 

42 

81 

"     2g 

2.00       " 

6 

28.0 

154 

3h.  oom. 

4676 

20 

82 

"     29 

3-25       " 

6 

JI..O 

M3 

4h.  25m. 

7  O23 

18 

85 

"     30 

9.55  A.M. 

7 

24.0 

132 

55m. 

i  290 

46 

86 

"     3° 

IO.I8       " 

7 

27.0 

148 

ih.  iSm. 

i  866 

58 

87 

"     30 

10-37       " 

7 

26.0 

'43 

ih.  37m. 

2330 

18 

88 

"     30 

11.17       " 

7 

28.0 

154 

2h.  I7in. 

3385 

15 

Sg 

"     3° 

12.25    I'-M. 

7 

27.0 

148 

3h.  25m. 

5  118 

10 

••     30 

1.40       " 

7 

24.0 

132 

4h.  4om. 

7052 

II 

93 

"     30 

3-22       " 

7 

28.0 

154 

6h.  22m. 

8629 

16 

97 

"     30 

4.30       " 

7 

7h.  30:11. 

10  689 

14 

I  OS 

"     31 

2.31       " 

8 

23.0 

126 

5h.  26m. 

6262 

9 

113 

Nov.  i 

12.07       ' 

8 

25.0 

137 

7h.  I2m. 

8  OK 

13 

I  I  [ 

"     i 

3-15     " 

8 

loh.  2om. 

12  23 

14 

Shut  outlet  3.15  r.M. 

IlS 

"     i 

4.03     " 

9 

22.0 

121 

38m. 

1062 

16 

I2C 

"     i 

4-33     " 

9 

22.0 

121 

ih.  o8m. 

I  732 

II 

124 

"      2 

11.07  A.M. 

9 

24.  c 

132 

2h.  52m. 

4099 

15 

I2t 

"      2 

12.31  r.M. 

9 

26.0 

143 

4h.  i6m. 

6  232 

14 

I2S 

"      2 

1.26     " 

9 

24.C 

132 

5h.  nm. 

7  599 

43 

130 

"       2 

3.48     " 

9 

24.  c 

132 

7h.  33m. 

9344 

19 

13. 

"     4 

2.32     " 

o 

26.  C 

143 

ih.  25m. 

i  802 

42 

135 

"     4 

3-37     " 

0 

27.  c 

148 

2h.  3Om. 

3474 

38 

13: 

"     5 

9.23  A.M. 

o 

24.  c 

132 

3h.  oim. 

4  i6c 

20 

"      5 

9.46       " 

o 

26.  c 

'43 

3h.  24m. 

4  73^ 

II 

142 

"     5 

IO.O7       " 

o 

3h.  45m. 

C   25 

10 

14: 

"     5 

10.32       " 

0 

25.  c 

137 

4h.  lom. 

5  82C 

12 

"     5 

11.30       " 

o 

24.  c 

132 

5h.  oSm. 

7  2IC 

14 

COMPOSITION  OF  OHIO  RIVER    WATER   AFTER  PURIFICATION.  129 

TABLE  No.  4. — Continued. 
Warren  System. 


Rat 

eof 

*j 

u 

Col 

ected. 

Filtr 

uion. 

£ 

i/i  . 

•J 

• 

^ 

M  <u 

Period  of 

•-  ^ 

^ 

1 

Number 

S. 

_o  a 

T3 

Last 

«3  Z 

i.  >• 

e 

Run. 

u  . 

5  "  ^ 

I 

Washing. 

'3-?\L 

O.U 

Remarks. 

5 

Date. 

Hour. 

£  tj 

it! 

Hours  and 
Minutes. 

Is'! 

P 

X 

o 

ia" 

1 

£ 

03 

151 

Nov.  5 

12.50  P.M. 

IO 

24.0 

132 

6h.  28m. 

9079 

13 

153 

5 

3-50   " 

IO 

16.0 

88 

9h.  28m. 

II  744 

10 

rcS 

"   6 

18 

I  50 

159 

6 

11.13   " 

II 

24.0 

132 

ih.  58m. 

2552 

15 

100 

6 

I.I9  P.M. 

II 

24.0 

132 

4h.  04111. 

5661 

17 

161 

6 

2.55  " 

II 

24.0 

132 

5h.  4om. 

7952 

24 

165 

"   7 

9.  10  A.M. 

II 

24.0 

132 

6h.  0301. 

8489 

138 

1  66 

7 

9.27   " 

II 

25.0 

137 

6h.  2om. 

8940 

82 

167 

7 

9-49  " 

II 

24.0 

132 

6h.  42m. 

9452 

54 

168 

7 

10.27   ' 

II 

24.0 

132 

7h.  2om. 

10385 

21 

173 

7 

11.25  A.M. 

II 

23.0 

126 

8h.  iSm. 

ii  725 

30 

175 

7 

12.24  P.M. 

12 

30.0 

16=; 

O2m. 

26 

196 

176 

7 

12.30   " 

12 

27.0 

148 

o8m. 

191 

54 

177 

7 

12.50   " 

12 

28.0 

154 

28m. 

751 

48 

178 

7 

I.og   " 

12 

24.0 

132 

47m. 

i  245 

61 

1  80 

7 

1-35  " 

12 

26.0 

143 

ih.  13111. 

1938 

46 

189 

7 

2.27  " 

12 

25.0 

137 

2h.  0501. 

3342 

31 

193 

7 

3.00  " 

12 

24.0 

132 

2h.  38m. 

4  180 

35 

197 

8 

9.50  A.M. 

12 

24.0 

132 

3h.  4301. 

5  "3 

49 

199 

8 

11.05   " 

12 

23.0 

126 

4h.  58m. 

6813 

42 

202 

"   8 

12  "*  7  P  M 

I  2 

6h.  30111. 

8  822 

K 

206 

"   8 

1  "'  j  1  '  • 
2.13 

13 

24.0 

132 

oym. 

152 

1  80 

208 

8 

2.27   " 

13 

23.0 

126 

2im. 

542 

70 

210 

"   8 

2.50   " 

13 

6.0 

33 

44m. 

i  050 

2f 

214 

"   9 

11.33  A.M. 

13 

24.0 

132 

ih.  22tn. 

2015 

4f 

218 

9 

1.27  P.M. 

13 

25.0 

137 

3h.  i6m. 

4802 

50 

221 

9 

2.30   " 

13 

24.0 

132 

4h.  igm. 

6328 

58 

227 

'  ii 

IO.47  A.M. 

13 

25.0 

137 

7h.  oim. 

10215 

224 

230 

"  ii 

II.  IO   " 

'3 

23.0 

126 

7h.  24m. 

10745 

136 

231 

"  ii 

2.32   " 

14 

24.  o 

132 

i  637 

41 

30-1 

'  '  25 

1  5 

35m 

I  58.1 

^J 
306 

"  25 

II.OO   " 

15 

24.0 

146 

ih.  I5m. 

i  096 

468 

3" 

11  25 

12.20  P.M. 

15 

20.0 

121 

2h.  35m. 

2  044 

390 

313. 

"  25 

1.40   " 

15 

21.  O 

127 

3h.  55m. 

3  °7: 

414 

315 

"  25 

3-30   " 

15 

25.0 

152 

5h.  45m. 

5732 

294 

318 

"  26 

9.28  A.M. 

15 

23.0 

I4O 

6h.  i8m. 

6745 

496 

322 

"  26 

10.20   " 

15 

21.  O 

127 

7h.  igm. 

7901 

372 

324 

"  26 

H-34   " 

15 

•:•<  LI 

121 

Sh.  24m. 

9437 

328 

326 

"  26 

2.IX)  P.M. 

"5 

20.0 

121 

loh.  5om. 

12445 

344 

332 

"  27 

9.27  A.M. 

15 

II.  O 

67 

nh.  52m. 

13667 

6Sc 

335 

"  27 

10.24   ' 

15 

18.0 

109 

I2h.  49m. 

14546 

452 

338 

'  27 

n-53  " 

'5 

25.0 

152 

I3h.  42m. 

15890 

446 

340 

"  27 

1.44  P.M. 

15 

23-5 

143 

I5h.  33m. 

18488 

564 

343 

'  27 

3-17   " 

15 

20.  o 

121 

I7h.  o6m. 

20  310 

512 

347 

'  29 

9.52  A.M. 

1  6 

II.  0 

67 

O2m. 

31 

I  302 

348 

'  29 

10.03   " 

1  6 

IO.O 

6  1 

I3m. 

132 

1  169 

349 

•  29 

10.14   " 

1  6 

IO.O 

61 

2401. 

248 

90! 

350 

'  29 

10.23   " 

1  6 

IO.O 

6  1 

33iii. 

355 

1092 

351 

'  29 

10.32   " 

16 

IO.O 

6  1 

42m. 

507 

876 

352 

'  29 

10.43   " 

16 

21.  O 

127 

53m. 

762 

760 

354 

'  29 

10.54   ' 

1  6 

2<).i 

121 

ih.  04111. 

I  006 

344 

356 

'  29 

1  2.  06  P.M. 

1  6 

23-5 

143 

2h.  i6m. 

2458 

624 

358 

'  29 

1.58   " 

1  6 

23.0 

140 

4h.  o8m. 

4968 

448 

368 

'  30 

IO.4I  A.M. 

16 

-  (•' 

I46 

7h.  17111. 

9416 

632 

370 

"  30 

11.51   " 

16 

•Jli.i 

158 

8h.  2710. 

u  043 

840 

372 

"  30 

1.39  P.M. 

16 

25.0 

152 

loh.  ism. 

13  691 

984 

376 

Dec.  2 

9.47  A.M. 

16 

20.  o 

121 

I2h.  ism. 

16  533 

77° 

378 

"    2 

10.48   ' 

16 

24.0 

I46 

I3h.  i6m. 

17949 

945 

381 

"    2 

12-35  P.M. 

16 

23.5 

143 

I5h.  O3m. 

20  462 

875 

383 

"    2 

2.38   " 

16 

23.0 

140 

I7h.  o6m. 

23  122 

i  078 

385 

3 

9  35  A.M. 

16 

25.0 

152 

i8h.  o6m. 

24401 

826 

WATER  PURIFICATION  AT  LOUISVILLE. 
TABLE  No.  4. — Continued. 

Warren  System. 


Rat 

.  Of 

S 

8 

Collected. 

Film 

tion. 

£ 

'<S1  . 

'Z 

^ 

u 

c  iJ 

Period  of 

*•  e 

fl 

Number 

8. 

S.  a 

•a 

Last 

Slcti 

^  si 

e 

3 

7, 

Date. 

Hour. 

Run. 

fc  3 

O  0  3 

its 

X 

Washing. 
Hours  and 
Minutes. 

||£ 

II 

Remarks. 

'C 

'fi 

=  O.B 

I 

~>4u 

u;j 

</) 

u 

S 

J 

U, 

CO 

1895 

387 

Dec.  3 

10.35  A.M. 

16 

25.0 

152 

igh.  o6m. 

25866 

532 

389 

3 

11.41   " 

1  6 

24-5 

149 

2oh.  I2m. 

27334 

665 

391 

3 

1.02  P.M. 

1  6 

22.  O 

133 

2ih.  33m. 

29349 

I  036 

392 

3 

2.O9   " 

1  6 

24.0 

146 

22h.  4om. 

30  929 

I  l6g 

Shut  inlet  2.  01  P.M.,  out 

395 

3 

3-00   " 

17 

21.0 

127 

I2m. 

213 

462 

let  2.21  P.M. 

396 

3 

3.10   " 

17 

22.  O 

133 

22m. 

401 

490 

397 

3 

3.2O   " 

17 

22.  O 

133 

32m. 

598 

392 

398 

3 

3-31   " 

I/ 

25.0 

152 

43m. 

836 

406 

399 

3 

3-4°  " 

17 

24.0 

146 

52m. 

i  036 

399 

400 

3 

3-50  " 

17 

21.  O 

127 

ih.  O2m. 

i  259 

399 

401 

3 

4-49  " 

17 

23.0 

140 

2h.  oim. 

2498 

334 

4<>3 

4 

10.40  A.M. 

17 

21.  O 

127 

3h.  49111. 

4898 

3i? 

405 

4 

II.06   " 

17 

2O.  O 

121 

4h.  ism. 

548J 

37S 

406 

4 

11.26   " 

17 

21.  O 

127 

4h.  35m. 

5908 

357 

407 

4 

11.45   " 

17 

22.0 

133 

4h.  54m. 

6315 

322 

408 

4 

1.  12  I'.M. 

17 

25.O 

152 

6h.  2im. 

8  281 

5iS 

409 

4 

2.52   " 

17 

21.  O 

127 

Sh.  oim. 

10591 

594 

412 

4 

4.19   " 

18 

24.0 

I46 

nm. 

321 

548 

413 

4 

4.29   " 

18 

22.  O 

133 

2im. 

533 

47" 

4i5 

4 

4.42   " 

18 

24.0 

I46 

34m. 

886 

320 

416 

4 

4.50   " 

18 

23.0 

140 

42m. 

95< 

3«* 

4'7 

4 

5.OO   " 

18 

2O.  O 

121 

52m. 

1136 

254 

418 

4 

5.II   " 

18 

23.O 

140 

ih.  03m. 

i  239 

280 

421 

"      ^ 

9.58  A.M. 

18 

2h.  oom. 

2  33' 

260 

423 

5 

10.42   " 

18 

24.0 

I46 

2h.  54m. 

3468 

1  80 

426 

5 

11.52   " 

18 

24.O 

I46 

3h.  54m. 

5  124 

236 

428 

5 

2.44  P.M. 

18 

24.O 

I46 

6h.  46m. 

g  161 

336 

435 

5 

3-40   " 

18 

24.0 

I46 

yh.  42m. 

10464 

472 

439 

6 

11.07  A.M. 

18 

22.  O 

133 

loh.  38m. 

13  12; 

386 

441 

6 

11.17   " 

18 

24.0 

I46 

loh.  48m. 

14727 

690 

444 

6 

12.50  P.M. 

19 

18.0 

log 

1  2m. 

131 

524 

445 

6 

I.OO   " 

19 

18.0 

109 

22m. 

295 

476 

446 

6 

I.IO   " 

19 

20.  o 

121 

32m. 

522 

476 

447 

0 

1.20   " 

19 

22.5 

126 

42m. 

738 

476 

448 

6 

1.30   " 

19 

23.0 

140 

52m. 

97< 

440 

45" 

6 

1.40   " 

19 

24.0 

I46 

ih.  O2m. 

i  175 

412 

451 

6 

3.3S   " 

19 

22.  O 

133 

3h.  oom. 

3934 

660 

454 

"   7 

10.17  A.M. 

19 

23.0 

140 

5)1.  5im. 

7932 

450 

456 

7 

12.27  P.M- 

19 

25.0 

152 

8h.  oim. 

ii  981 

412 

459 

7 

3-5<>   " 

20 

23.0 

140 

nm. 

182 

254 

462 

9 

10.10  A.M. 

20 

20.  o 

121 

2h.  1  901. 

3082 

324 

464 

9 

11.14   " 

20 

21.0 

127 

3h  23m. 

4445 

250 

466 

9 

12.17  I'.M- 

2O 

24.0 

I46 

4h.  26m. 

5  7<>5 

270 

469 

9 

i-57  " 

20 

24.0 

I46 

6h.  o6m. 

8o6c 

272 

47i 

9 

3-3°  " 

20 

24.0 

I46 

7h.  39m. 

1037 

324 

475 

'   o 

9.17  A.M. 

2O 

23-' 

I4O 

gh.  I3m. 

12  8IC, 

312 

477 

"   o 

0.  2O   " 

20 

23.O 

140 

loh.  i6m. 

14  oil 

406 

484 

"    0 

2.23  P.M. 

2 

22.0 

133 

2om. 

325 

288 

485 

"   o 

2-33   " 

2 

21.  O 

127 

3Om. 

53< 

344 

486 

"   o 

2.43  " 

2 

2O.  O 

121 

4om. 

779 

330 

487 

0 

2-53  " 

2 

22.0 

133 

5om. 

i  032 

324 

488 

"   o 

1.03  " 

2 

24.0 

I46 

ih.  oom. 

i  247 

246 

489 

"   o 

1.13  " 

2 

24.0 

I46 

ih.  lorn. 

1494 

1  88 

49  1 

"    0 

2.10   " 

2 

24.0 

I46 

2h.  O7m. 

2845 

266 

493 

"   o 

3-24   " 

2 

24.0 

I46 

3h.  2im. 

4564 

244 

496 

"   I 

9.24  A.M. 

2 

24.0 

I46 

5h.  3im. 

7489 

196 

498 

"   I 

II.  II   " 

2 

24.0 

I46 

7h.  l8m. 

9994 

210 

500 
502 

"   I 
"   I 

12.  l8  P.M. 
I.lS   " 

2 
2 

23.O 
2O.  O 

140 
121 

8h.  25m. 
gh.  25m. 

ii  56 
12  92; 

I96 
2O2 

Shut  inlet  1.18  P.M.,  out 

505 

"   I 

2.5S   " 

2 

21.0 

127 

54m. 

i  137 

I46 

let  i.  21  P.M. 

509 

"    2 

9.40  A.M. 

2 

24.0 

I46 

4h.  07m. 

5452 

128 

COMPOSITION  OF  OHIO  RIVER    WATER   AFTER   PURIFICATION. 


TABLE  No.  4. — Continued. 
Warren  System. 


Rate  of 

S 

S 

Collected. 

Filtration. 

£ 

K 

| 

. 

U 

1/5  ii 

Period  of 

u  5f 

u  > 

J& 

Number 

Q. 

o  ex 

•d 

ServiceSinc 

"  !H  ** 

g 

w 

"S  w  " 

u 

Last 

'_r  **    tj 

4>  ~ 

Remarks. 

3 

Run 

V    -J 

O  S  = 

X 

Washing. 

*gfc 

a  6 

"Z. 

Date. 

Hour. 

tl 

13 

Hours  and 
Minutes. 

*-     V-  •& 

SS 

•q 

II 

—    (J    „ 

§ 

~.3u 

rt  U 

X 

u 

sa" 

,J 

E 

m 

1895 

5" 

Dec.   12 

12.04  P'M- 

22 

24.0 

146 

6h.  3im 

8  85 

228 

513 

"         12 

3-05      " 

23 

22.  C 

133 

ih.  oim 

I  273 

igc 

518 

"         13 

IO.I6  A.M. 

23 

22.  C 

133 

4h.  4Om 

6i8c 

1  08 

521 

13 

4.38  P.M. 

24 

22.  C 

133 

52m 

1073 

136 

525 

14 

lO.Og  A.M. 

24 

23.  c 

140 

2h.  52m 

3811 

108 

527 

14 

12.59  P-M- 

24 

23. 

140 

5h.  42m 

7672 

135 

53i 

14 

3-33     " 

25 

20. 

121 

I4m 

281 

274 

534 

"         If) 

9.30  A.M. 

25 

21. 

127 

2h.  25m. 

3  log 

160 

536 

"       16 

11-37      " 

25 

23- 

140 

4h.  32m. 

6  09. 

126 

538 

"       16 

2.31    P.M. 

25 

21. 

127 

7h.  26m. 

9961 

172 

54' 

"       16 

5.17      " 

26 

23. 

140 

ih.  o8m. 

1492 

1  20 

543 

"       17 

9.30  A.M. 

26 

23. 

140 

ih.  5om. 

2430 

ill 

546 

17 

12.58  P.M. 

26 

23- 

140 

5h.  i8m. 

7156 

170 

548 

.     "       17 

3.21       " 

27 

23. 

140 

ih.  o6m. 

I  260 

no 

551 

17 

4-37     " 

27 

22. 

133 

2h.  22m. 

3001 

148 

554 

"       18 

g.2O  A.M. 

27 

22. 

133 

3h.  4om. 

4731 

197 

556 

"       18 

10.41      " 

27 

23- 

140 

5h.  oim. 

6  509 

196 

558 

"       18 

1.16     " 

27 

'33 

7h.  36m. 

9382 

185 

559 

"       18 

2.32     " 

28 

22. 

133 

I3m. 

234 

236 

560 

"       18 

2.42     " 

28 

22.  0 

133 

23m. 

444 

294 

56i 

"       18 

2.52     " 

28 

22.0 

'33 

33m. 

658 

274 

562 

"       18 

3-02      " 

28 

22.0 

133 

43m. 

874 

2  2O 

563 

"       18 

3.12   " 

28 

2.O 

133 

53m- 

i  098 

I78 

565 

"       18 

3.22   " 

28 

2.0 

133 

ih.  03111. 

i  306 

278 

568 

"       18 

4-39     " 

28 

3-° 

140 

2h.  2om. 

2  g64 

I58 

57° 

"       '9 

9.25     " 

2S 

3-0 

140 

3h.  3im. 

4474 

l6g 

580 

'9 

3.23  P.M. 

28 

4.0 

146 

7h.  39111. 

IO  212 

142 

582 

19 

4.40    " 

28 

4.0 

146 

8h.  56m. 

11987 

165 

587 

1       20 

10.14  A.M. 

29 

I.O 

127 

I2m. 

234 

426 

589 

20 

11.59     " 

29 

4.0 

146 

ih.  57m. 

2  590 

103 

591 

20 

2.  02  P.M. 

29  ' 

3-o 

i  |n 

4h.  oom. 

5  397 

188 

594 

"         2O 

3-53     " 

29 

4-0 

146 

5h.  sim. 

7902 

720 

597 

"         21 

g.ig  A.M. 

29 

I.O 

127 

7h.  47m. 

10460 

344 

600 

"         21 

4-01      " 

30 

2.0 

133 

3h.  3im. 

4  627 

164 

603 

"         23 

9.18      " 

30 

2.O 

73 

5h.  I4m. 

6551 

260 

606 

;         23 

10.39      " 

30 

g.O 

H5 

6h.  35m. 

7  754 

150 

612 

23 

12.34  P.M. 

30 

o.o 

121 

8h.  3om. 

9932 

132 

616 

'         23 

3-33     " 

30 

8.0 

49 

nh.  2gm. 

13316 

150 

Shut  inlet  3.20  P.M.,  out 

619 

24 

9.29A.M. 

31 

3.0 

140 

ih.  4gm. 

2466 

63 

let  3.40  P.M. 

627 

24 

12.48    P.M. 

31 

4.0 

146 

5h.  o8m. 

6433 

78 

628 

24 

3.07      " 

31 

I.O 

127 

7h.  27m. 

9772 

86 

637 

"         26 

lO.Og  A.M. 

31          22.  0 

133 

toh.  48m. 

13578 

95 

638 

"         26 

11.49      " 

32          22.  O 

133 

32m. 

688 

59 

639 

"         26 

12.04  !'-M. 

32 

23.0 

140 

47m. 

994 

60 

644 

"         26 

3-49      " 

32 

22.0 

133 

4h.  32tn. 

6i34 

244 

651 

"         27 

IO.O7  A.M. 

32 

21.  O 

127 

7h.  ism. 

9392 

i  701 

655 

'         27 

12.34  P.M. 

32 

21.  O 

127 

gh.  4201. 

12  757 

i  530 

660 

"         27 

2-57      " 

32 

I2h.  05111. 

15  815 

924 

Shut  outlet  2.57  P.M. 

665 

"         27 

3-42     " 

33 

24.0 

146 

3001. 

641 

230 

666 

27 

3-57     " 

33 

22.0 

133 

45m. 

978 

128 

671 

'         27 

4-55     " 

33 

22.  O 

133 

ih.  43111. 

2  223 

1  60 

674 

"        28 

9.56  A.M. 

33 

22.0 

133 

3h.  iim. 

4131 

428 

682 

"     28 

11.56     " 

33 

21.0 

127 

5h.  iim. 

6776 

i  728 

683 

28 

3.06  P.M. 

-IT 

8h.  2im. 

II  Oil 

I  350 

Shut  inlet  3.04  P.M.,  out 

692 

"       30 

10.56  A.M. 

JJ 

34 

22.  0 

133 

2h.  3im. 

2  884 

402 

let  3.24  P.M. 

696 

'       30 

12.15  r-M. 

35 

21.  0 

127 

14111. 

179 

474 

697 

1       30 

12.44     " 

35 

22.0 

133 

43m. 

804 

2IO 

7'" 

'       30 

1-59     " 

35 

24.0 

146 

ih.  58m. 

2  561 

502 

705 

1       30 

4-53     " 

36 

23.0 

140 

l8m. 

378 

210 

707 

'       3« 

5.,  6    " 

3f> 

22.0 

133 

4im. 

959 

170 

711 

31 

10.45  A.M. 

36 

23.0 

140 

2h.  34tn. 

4708 

406 

• 

WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  4. — Continued. 

Warren   System. 


Rate  of 

ti 

0 

Collected. 

Filtration. 

fc 

1 

•J 

V 

Number 

g_ 

1  s. 

T3 

Period  of 

Service  Since 

1  1  . 

u  u. 

E 

of 

*j 

"^    V    rr 

5 

Last 

•  rt  f-  •} 

v  ~ 

Remarks. 

p 

Run. 

OJ   0; 

6  s  3 

X 

Washing. 

"*  «-  k* 

a 

£ 

Date. 

Hour. 

fc  5 

Hours  and 

1;  ~'~ 

T'S 

~n 

.y  c 

.2  v-" 

VI 

Minutes. 

v  £  "a 

^  £ 

X 

\7. 
u 

5  a? 

§ 

--(-) 

n 

1895 

717 

Dec.    31 

1.39  P.M. 

37 

17.0 

103 

I5m. 

215 

440 

718 

"      31 

2.09      " 

37 

23.0 

140 

45m. 

835 

278 

1896 

730 

Jan.       2 

10.56  A.M. 

38 

22.5 

136 

lorn. 

130 

784 

731 

2 

11.26      " 

38 

25.0 

152 

4om. 

690 

600 

740 

"          2 

2.40  P.M. 

38 

18.0 

109 

3)1.  54111. 

5  260 

i  400 

743 

"           2 

4.06      " 

39 

20.  0 

121 

I5m. 

222 

405 

749 

3 

IO.2I  A.M. 

39 

21.0 

127 

3h.  0701. 

3722 

i  So 

753 

3 

1.22  P.M. 

40 

2O.  O 

121 

iSm. 

I  86 

220 

754 

3 

I.58      " 

40 

2O.5 

124 

5im. 

956 

97 

765 

4 

11.55  A.M. 

41 

18.0 

109 

I4m. 

118 

I/O 

772 

4 

2.26  P.M. 

21.5 

130 

2h.  45m. 

2558 

133 

776 

6 

11.55  A.M. 

42 

17.0 

103 

3om. 

415 

1  02 

780 

6 

3.27   P.M. 

42 

17.0 

103 

4h.  O2m. 

3891 

112 

785 

7 

12.24      " 

43 

14.0 

85 

4h.  igm. 

4  159 

43 

789 

7 

3-52      " 

44 

12.0 

73 

2h.  I7m. 

2  218 

66 

794 

8 

11.58  A.M. 

45 

16.0 

97 

55m. 

858 

25 

799 

8 

2.28  P.M. 

45 

16.0 

97 

3h.  2501. 

3235 

68 

802 

8 

2.49      " 

45 

16.0 

97 

3h.  46m. 

3529 

84 

809 

9 

IO.2I  A.M. 

46 

18.0 

1  09 

2h.  2sm. 

2  316 

10 

814 

9 

1.26  P.M. 

47 

16.5 

IOO 

1501. 

21O 

53 

816 

9 

1.47     " 

47 

15.0 

gl 

36m. 

500 

21 

826 

10 

1.05     " 

48 

14.0 

85 

09  m. 

119 

152 

827 

"       10 

1.42     " 

48 

15.0 

9' 

46m. 

699 

36 

836 

"       ii 

II.  21  A.M. 

49 

17-5 

1  06 

2h.  53111. 

2  630 

36 

843 

"       13 

12.30  P.M. 

51 

16.0 

97 

15111. 

198 

35 

844 

13 

1.  00      " 

51 

15.0 

91 

45m. 

f>33 

31 

846 

;       13 

2.OI      " 

51 

16.0 

97 

ih.  46m. 

i  608 

10 

850 

'3 

4-57      " 

52 

16.0 

97 

i  SRI. 

207 

78 

856 

14 

11.56  A.M. 

52 

17.0 

103 

3h.  44in. 

3516 

M 

859 

14 

1.57  r.M. 

53 

16.0 

97 

I5m. 

186 

31 

863 

'4 

2.27    " 

53 

17.0 

103 

45m. 

7'4 

32 

867 

'4 

3-25     " 

53 

17.0 

103 

ih.  4301. 

i  606 

25 

871 

15 

10.40  A.M. 

54 

16.0 

97 

ISm. 

181 

62 

875 

T5 

II.  10     " 

54 

16.0 

97 

45m. 

657 

12 

879 

15 

12.59  r.M. 

54 

16.0 

97 

2h.  34111. 

2327 

4g 

88  1 

"       15 

2.54    " 

54 

14.0 

85 

4)1.  2gm. 

4  124 

77 

886 

"       16 

10.43  A.M. 

55 

16.5 

IOO 

2h.  34m. 

2356 

78 

891 

"       16 

12.58  P.M. 

55 

14.0 

85 

4h.  4gm. 

4486 

94 

896 

"       16 

2.17      " 

56 

16.0 

97 

15111. 

203 

73 

897 

"       16 

2.47     " 

56 

16.5 

IOO 

45m. 

663 

60 

898 

"       16 

2.59     " 

56 

16.0 

97 

57m. 

853 

58 

915 

"       17 

11.37  A.M. 

57 

17.0 

103 

15111. 

176 

126 

920 

17 

I2.O7  P.M. 

57 

17.0 

103 

45m. 

675 

924 

17 

1.02      " 

57 

16.0 

97 

ih.  4om. 

'  5'5 

'"65 

931 

17 

2.  II      " 

57 

15.0 

91 

2h.  4gm. 

2  615 

i/i 

935 

"        17 

3-53      " 

58 

"7-5 

1  06 

1  7m. 

240 

82 

939 

;        17 

4.23      " 

58 

15.0 

91 

47m. 

660 

76 

941 

17 

4.58      " 

58 

16.0 

97 

ih.  22m. 

I   205 

68 

943 

"       18 

IO.O8  A.M. 

58 

16.0 

97 

2h.  54m. 

2  620 

38 

952 

"       18 

I.  CO  P.M. 

59 

16.0 

97 

15111. 

217 

67 

956 

"       18 

1.30      " 

59 

14.0 

85 

45m. 

677 

70 

961 

"      18 

2.50      " 

59 

15-5 

94 

2h.  05111. 

1887 

64 

968 

"         20 

10.38  A.M. 

60 

15.0 

9' 

2h.  iSm. 

204O 

102 

971 

"         20 

2.05  P.M. 

61 

16.0 

97 

I5m. 

176 

1  08 

973 

"        2O 

4.09      " 

61 

15.0 

91 

2h.  igm. 

2086 

146 

982 

"        21 

12.10     " 

62 

16.0 

97 

15111. 

181 

86 

983 

"         21 

12.40     " 

62 

16.0 

97 

45m. 

691 

32 

985 

"         21 

4.12      " 

63 

16.0 

97 

34m. 

453 

36 

99' 

22 

g.2I  A.M. 

63 

16.0 

97 

2h.  17111. 

2073 

33 

997 

"        22 

2.12  P.M. 

64 

17.0 

103 

ih.  35111. 

1464 

36 

1028 

"        25 

2.27      " 

65 

ig.o 

2h.  O3m. 

2418 

60 

COMPOSITION  OF  OHIO  RIVER    WATER   AFTER   PURIFICATION. 


133 


TABLE    No   4.— Continued. 

Warren  System. 


Rate  of 

_• 

u 

Collected. 

Filtration. 

S 

c 

u 

fc. 

.5 

& 

Number 

S. 

!«• 

Period  of 
Service  Since 

S|- 

3 

o  u. 

E 

of 

—  a  y 

u 

Last 

>   rt   4J 

£  - 

Remarks. 

a 

Run. 

,**£ 

6  S  I 

K 

Washing. 
Hours  -  nd 

fek 

K'E 

J 

Date. 

Hour. 

*  | 

0*^3 

^ 

Minutes. 

"  5  'S 

£s 

•e 

2jg 

is.? 

i 

=  JU 

"u 

(/> 

<•> 

s 

U. 

n 

1895 

032 

Jan.    27 

10.03  A.M. 

f>5 

16.0 

97 

5h.  52m 

6  108 

II- 

°37 

'       27 

11.22      " 

66 

16.0 

97 

15111 

216 

39 

038 

'       27 

11.52      " 

66         16.0 

97 

45m 

666 

177 

039 

1       27 

1.05   I'.M. 

66 

ii,  .1 

97 

ih.  sSm. 

1836 

41 

044 

'       27 

4.06       " 

66 

15.0 

91 

4h.  sgm. 

4636 

412 

050 

"       28 

9.45  A.M. 

67 

16.5 

100 

ih.  2gm. 

i  226 

225 

"57 

"       28 

3-33  I'-M. 

68 

15-0 

gl 

ih.  lorn. 

954 

536 

058 

"       28 

4.29     " 

68 

16  o 

97 

2h.  o6m. 

I  924 

650 

065 

1       29 

10.09  A.M. 

68 

16.0 

97 

3  h.  sSm. 

3504 

327 

068 

'      29 

1.55   I'-M. 

69 

15-0 

91 

ih.  55m. 

i  828 

570 

071 

'       29 

5-15      " 

70 

14-' 

85 

I7m. 

219 

679 

074 

'      3° 

10.56  A.M. 

7" 

14.0 

85 

2h.  28m. 

2  279 

79 

076 

"       30 

12.56  P.M. 

70 

14.0 

85 

4h.  2Sm. 

4259 

76 

079 

'       30 

2.54      " 

71 

15-5 

94 

5&m. 

648 

58 

083 

'       31 

10.42  A.M. 

71 

10.  0 

61 

5h.  I4m. 

4788 

169 

A.  Shut  inlet  10.42  A.M.. 

090 

'      31 

2.42  P.M. 

72 

7O.O 

121 

2h.  O5m. 

1998 

59 

outlet  10.56  A.M. 

092 

'       31 

3-43     " 

72 

16.0 

97 

3h.  oom. 

2948 

55 

095 

Feb.      i 

9-57  A.M. 

72 

16.0 

97 

5h.  46m. 

5298 

85 

096 

"        i 

12.  II   I'.M. 

73 

16.0 

97 

47m. 

699 

39 

099 

"        i 

2.40      " 

73 

16.0 

97 

3h.  i6m. 

2959 

69 

103 

i 

4-55     " 

74 

14.0 

85 

3om. 

415 

30 

107 

3 

10.12  A.M. 

74 

16.0 

97 

2h.  3om. 

22Q5 

174 

no 

3 

1.10  I'.M. 

74 

16.0 

97 

5h.  ism. 

4875 

196 

116 

3 

4-55     " 

75 

17.0 

103 

ih.  i8m. 

I  140 

225 

121 

4 

10.12  A.M. 

75 

15-5 

94 

3h.  O5m. 

2  850 

240 

124 

4 

II-45     " 

75 

16.0 

97 

4h.  3801. 

4290 

606 

127 

4 

2.25  P.M. 

75 

16.0 

97 

7h.  i8m. 

6730 

555 

131 

4 

5-13      " 

76 

16.0 

97 

ih.  24m. 

I  273 

4740 

I36 

5 

lO.Og  A.M. 

76 

18.0 

109 

2h.  5im. 

2873 

256 

140 

5 

"•45     " 

76 

18.0 

109 

4h.  27111. 

4513 

752 

144 

5 

3.O2   P.M. 

77 

16.0 

97 

2h.  3om. 

2570 

510 

149 

5 

5-04       " 

78 

14.0 

85 

05111. 

29 

816 

155 

6 

1O.05  A.M. 

78 

17.0 

103 

ih.  36m. 

I  339 

232 

161 

6 

12.19  I'.M. 

78 

17.0 

103 

3h.  som. 

3519 

173 

163 

6 

3-10      " 

79 

17.0 

103 

34m. 

43' 

207 

1  68 

6 

4.12      " 

79 

16.5 

IOO 

ih.  36111. 

i  421 

270 

173 

7 

10.10  A.M. 

79 

16.0 

97 

4h.  ogm. 

3  701 

237 

177 

7 

1.25    P.M. 

80 

16.0 

97 

ih.  33m. 

i  646 

338 

183 

7 

5.22       " 

Si 

16.0 

97 

ih.  oom. 

886 

512 

187 

8 

10.27  A.M. 

81 

16.0 

97 

2h.  I7m. 

2049 

55f> 

191 

8 

2.10  P.M. 

82 

16.0 

97 

43m. 

677 

194 

195 

8 

3.00      " 

82 

18.0 

109 

ih.  27111. 

1417 

1  80 

198 

8 

4.46       " 

82 

14.0 

85 

3h.  1301. 

3047 

53<> 

203 

"          IO 

10.12  A.M. 

82 

16.0!     97 

4h.  57m. 

4797 

275 

207 

"         10 

12.56   P.M. 

83 

ifi.o 

97 

54m. 

800 

no 

211 

"          IO 

3.10      " 

83 

14.0 

85 

3h.  oSm. 

2980 

384 

Shut  inlet  3.03  P.M.,  out 

215 

"         IO 

4-57       " 

84 

17.0 

°3 

57m. 

862 

348 

let  3.23  P.M. 

258 

"     13 

2-34     " 

85 

21 

23m. 

468 

182 

263 

13 

5.19     " 

85 

19.0 

15 

3h.  oSm. 

3  588 

678 

I).   Application  of  chemi 

265 

14 

10.19  A.M. 

85 

19.  o 

15 

4(1.  23m. 

4928 

I  670 

cals  unsatisfactory: 

269 

14 

1.  12  P.M. 

86 

21.  0 

27 

ih.  44m. 

2047 

57 

chemical   meter  out 

273 

14 

3-14      " 

86 

19-5 

18 

2h.  58111. 

3457 

40 

of  order. 

283 

15 

IO.O7  A  M. 

86 

21.  O 

27 

4(1.  23m. 

5<x>7 

84 

287 

15 

1.25   P.M. 

8? 

22-5 

36 

ih.  torn. 

1487 

go 

291 

15 

2-57     " 

87 

20.  o 

21 

2h.  42m. 

3397 

243 

295 

15 

5.24   " 

88 

19.0 

15 

ih.  32m. 

1673 

302 

17 

IO.06  A.M. 

88 

20.0 

21 

2h.  54m. 

4  173 

log 

306 

17 

1.35    P.M. 

89 

•I." 

IS 

33m. 

521 

125 

310 

17 

3.07       " 

89 

20.  O 

21 

2h.  osm. 

2  311 

87 

320 

iS 

1O.2O  A.M. 

90 

V.I 

09 

3om. 

550 

20 

324 

18 

11-55     " 

90 

I9.O 

15 

2h.  osm. 

2  260 

56 

'34 


WATER   PURIFICATION  AT  LOUISVILLE. 
TABLE  No.  4. — Continued. 

Warren  System. 


Ka 

e  of 

- 

u 

Collected. 

Filtr 

s 

c 

u 

—  — 

b. 

Period  of 

*% 

£ 
(_j 

\ 

Number 
of 

- 

gs.  _ 

•0 

d 

"''Tast'"" 
W;islnnR. 

js.™fc 

Remarks. 

3 

Kun. 

*>  ~ 

ojji  g 

PH 

Until  sand 

•0^0 

A  8 

55 

D:ite. 

Hour. 

0   1 

i.= 

'o 

Minutes. 

t  £ 

~ 

'• 

Us.? 

i 

1,33 

«  U 

% 

U 

*?. 

j 

h 

CO 

1895 

1328 

Feb.   IS 

2.  2O  I'.M.                , 

9° 

7.0 

103 

4!).  3om. 

4790 

198 

1333 

"     18 

4-55      " 

9' 

8.0 

109 

ih.  39m. 

I  804 

67 

i  en 

"      1  8 

5.05      " 

9' 

18.0 

109 

ih.  49111. 

'  954 

Oi 

i  ;i  ; 

"     i<) 

10.  12  A.M. 

9' 

9.0 

"5 

3h.  ism 

3434 

39 

1347 

'      '9 

11.31      " 

9' 

S.i 

109 

4h.  34111. 

4894 

104 

1351 

'      '9 

3.04  r.M. 

92 

18.5 

112 

ih.  42111. 

i  829 

55 

1358 

'      '9 

5.10    " 

Q2 

iS.o 

109 

3)1.  4801. 

4069 

382 

1362 

"     20 

II  .OO  A.M. 

92 

iS.o 

109 

5h.  43m. 

6029 

156 

1  (06 

"      20 

12.03    I'.M. 

93 

iS.o 

109 

15111. 

209 

116 

1368 

"      20 

12.18       " 

93 

18.0 

109 

30  m. 

459 

104 

1369 

"      20 

I2-33     " 

93 

18.0 

log 

45111. 

739 

287 

1370 

"      2O 

12.40    " 

93 

18.0 

109 

52111. 

i  009 

560 

1371 

"      2O 

1.04     " 

93 

18.0 

109 

ih.  i6m. 

1309 

79 

1375 

"      20 

2.06     " 

93 

18.0 

109 

2h.  i8m. 

2389 

135 

1377 

"      20 

3.08     " 

93 

17.0 

103 

3h.  2om. 

3469 

MI 

1382 

"       20 

4.08     " 

93 

17.  ( 

103 

4h,  2om. 

4489 

325 

1387 

"      20 

5-'5     " 

94 

17-5 

1  0() 

oSm. 

90 

200 

i  ;.>» 

"       21 

9.5*.  A.M. 

94 

16.5 

100 

Ih.  2om. 

i  330 

48 

i  ;<>! 

"       21 

12.42  r.M. 

'14 

17.0 

103 

4)1.  o6m. 

4  160 

34 

i  I'M 

"       21 

5-°9     " 

95 

18.5 

I  12 

14111. 

227 

"47 

i  |c>S 

"       22 

10.20  A.M. 

95 

18.0 

109 

ih.  55in. 

2077 

88 

M" 

"       22 

1  .  1  8  r.M. 

95 

18.0 

R>) 

4)1.  53m. 

5337 

"5 

1412 

"       22 

3.01     " 

95 

19.' 

115 

6h.  3(>m. 

7  '77 

528 

M'4 

"       22 

4-53     " 

96 

'7-5 

1  06 

ih.  14m. 

'  3'5 

94 

1422 

"       24 

10.27  A.M. 

96 

17-5 

U)6 

3h.  1701. 

3480 

79 

'423 

"       24 

i  .  10  r.M. 

96 

18.5 

112 

Oh.  oom. 

0440 

77 

M3' 

"       24 

5.16     " 

97 

18.5 

I  12 

ih.  35111. 

i  On 

02 

'437 

!'  25 

10.26A.M. 

97 

20.  o 

121 

3)1.  lOin. 

3631 

4" 

'44' 

-5 

1.14  I'.M. 

98 

19.0 

U5 

48111. 

734 

52 

'445 

3.07    " 

98 

'7-5 

1  06 

ah.  41111. 

2  824 

0.( 

1452 

"  25 

5.08  " 

98 

18.5 

112 

4h.  42m. 

4994 

'27 

1456 

"        2f> 

10.2(>  A.M. 

»s 

"7-5 

1O6 

(>h.  3001. 

0904 

122 

1460 

"       2(> 

n.43    " 

98 

15.0 

9' 

7h.  47111. 

8  214 

294 

1464 

"       26 

3.04    P.M. 

99 

18.0 

109 

ih.  47111. 

1823 

OS 

147' 

"       2t> 

5.23       " 

99 

iS.o 

109 

4h.  06111. 

4363 

326 

1478 

"       27 

10.3(1  A.M. 

99 

18.0 

109 

5h.  49m. 

0  193 

34 

M79 

27 

1.43  r.M. 

00 

=4-5 

'49 

44111. 

923 

30 

i  r  i 

2.58    " 

oo 

24.0 

146 

ih.  59111. 

2  773 

53 

1488 

"       27 

5.07    " 

01 

23.0 

140 

17111. 

34' 

'4- 

1490 

"       28 

10.3!)  A.M. 

01 

25.' 

152 

2)1.  lOm. 

33" 

21 

1502 

"       28 

3.23   I'.M. 

02 

25.  ( 

152 

ih.  56m. 

i  241 

33 

1507 

"       28 

5.00      " 

02 

23.5 

'43 

3h.  33111. 

4961 

4'3 

1512 

"       2C) 

10.30  A.M. 

03 

-••..> 

I5Z 

ih.  29111. 

2  320 

138 

1516 

•'       29 

1.34   I'.M. 

"4 

-'I  > 

146 

24111. 

494 

170 

1520 

29 

3-14      " 

"4 

25.0 

152 

ah.  04111. 

3024 

187 

1528 

"       29 

5.15      " 

05 

24.0 

146 

17111. 

396 

211 

113' 

Mar.    2 

9.33A.M. 

i>5 

-•-'.- 

135 

ill.  03111. 

i  6oO 

I30 

1536 

2 

10.21       " 

05 

25.0 

152 

ih.  51111. 

a  766 

33' 

1540 

"          2 

1.33   P.M. 

01) 

24.5 

M9 

ih.  o7m. 

i  549 

1544 

"          2 

3.12      " 

Of) 

-••••' 

140 

ah.  40m. 

3859 

676 

1549 

2 

5.00      " 

»7 

25.0 

152 

22m. 

457 

333 

'557 

3 

10.37  A.M. 

07 

24.0 

146 

2h.  23111. 

3  547 

'55 

1561 

3 

12.15  r.M. 

07 

24.0 

146 

4)1.  oim. 

5897 

405 

'5<>5 

3 

3-io    " 

08 

25.0 

152 

ih.  27111. 

2025 

95 

1570 

"       3 

5.10     " 

08 

24.0 

146 

3h.  2701. 

4845 

553 

I57& 

4 

10.44  A.M. 

oS 

21-5 

130 

4h.  54in. 

0999 

005 

1581 

4 

12.58  I'.M. 

09 

23.0 

140 

ih.  14111. 

i  747 

So 

1584 

4 

3.19     " 

09 

24.1 

146 

3h.  35m. 

5093 

i  39. 

1589 

4 

5  °3     " 

10 

-'  1  •' 

146 

ih.  05111. 

1452 

116 

1595 

5 

10.30  A.M. 

10 

25.  t 

152 

3h.  02m. 

4442 

187 

I  599 

"       5 

12.49  r.M. 

II 

23.0 

140 

43111. 

930 

93 

lOob 

5 

3.29  •• 

II 

23.0 

140 

3h.  23111. 

4050 

590 

COMPOSITION  OF  OHIO  RIVER    WATER   AFTER   PURIFICATION. 
TABLE  No.  4. — Continued. 

Warren  System. 


'35 


Rate  of 

j 

s 

Collected. 

Filtration. 

[i. 

£ 

Jj 

Number. 

I 

IS. 

Period  of 
service  Since 

fc  c1 

3 
O  ^ 

a 

25 

of 

Sc 

Ill 

I 

Last 
Washing. 
Hours  and 

tl! 

s.5 

2a 

Remarks. 

Date. 

Hour. 

o  c 

;  1.3: 

*o 

Minutes. 

sa's 

5  c 

•3 

IS 

is 

JJ<3 

%•" 

« 

u 

Ji 

j 

b 

m 

1895 

1612 

Mar.     5 

5.18  r.M. 

112 

!6.0 

158 

iom. 

169 

615 

1616 

6 

IO.32  A.M. 

112 

!3-o 

140 

ih.  54111.    2  819 

48 

1621 

6 

12.38    P.M. 

112 

23.0 

140 

4)1.  oom.     5  699 

615 

1625 

6 

3.l6       " 

H3 

26.0 

158 

ih.  51111. 

2737 

106 

1633 

"       6 

5-25     " 

H4 

24.5 

149 

37"'- 

808 

59 

1637 

7 

10.40  A.M. 

114 

24.0 

146 

2li.  2om. 

3468 

39 

1641 

7 

12.53   l'-M. 

114 

23.0 

140 

4h.  33tn. 

6  508 

485 

If'44 

7 

3.10      " 

»5 

24.0 

146 

ih.  i6m. 

I  750 

40 

1649 

7 

5-15       ' 

115 

24.0 

146 

3h.  2im. 

4  710 

154 

1656 

9 

10.58  A.M. 

H5 

23.5 

M3 

5h.  33111. 

7890 

620 

1  66  1 

9 

12.5O    I'.M. 

116 

24.5 

149 

ih.  i6m. 

I  738 

40 

1670 

9 

3-40       " 

i'7 

24.0 

146 

3(1111. 

837 

35 

1671 

9 

5.04       ' 

117 

24.0 

146 

2h.  oom. 

2757 

64 

1678 

'     10 

IO.I9  A.M. 

"7 

24.0 

146 

3h.  45m. 

5  357 

139 

1682 

"        10 

1.33   I'.M. 

US 

25.0 

152 

ih.  43m. 

2344 

68 

1686 

"     10 

3-07     " 

18 

24.5 

149 

3h.  17111. 

4605 

935 

1693 

"     10 

5.15     ' 

'9 

25.0 

152 

ih.  29111.    2  085 

61 

1699 

"     ii 

IO.I8  A.M. 

'9 

25.0 

152 

3]].  <)2m. 

4375 

300 

1706 

"     ii 

3.17    P.M. 

21 

20.0 

121 

ih.  34m. 

I  872 

310 

1713 

"     ii 

5.05       ' 

22 

21.5 

130 

29111. 

562 

60 

1719 

"       12 

10.15  A.M. 

22 

19-5 

118 

2h.  09111. 

2  622 

89 

1723 

"        12 

12.54    I'-M' 

23 

9.0 

H5 

ih.  igm. 

I  439 

26 

1727 

"       12 

3.22       " 

23 

7.5 

1  06 

3h.  47m. 

4069 

485 

1732 

"       12 

5.oS     " 

24 

20.0 

121 

ih.  07m. 

I  311 

24 

1739 

"       '3 

IO.23  A.M. 

24 

8.5 

112 

2h.  55m. 

3  551 

137 

1743 

'       13 

1.09    P.M. 

25 

9-5 

us 

ih.  17m. 

1389 

26 

1747 

'        '3 

3-10       " 

25 

18.5 

112 

3h.  i8m. 

3639 

I  OOO 

1752 

'        13 

5.OI    P.M. 

26 

19.5 

n8 

ih.  1301. 

i  377 

1  1 

1758 

'       M 

IO.27  A-M' 

26 

18.5 

112 

3h.  09111. 

3827 

137 

1764 

'      «4 

1.  06    P.M. 

127 

19.0 

US    •••• 

ih.  2im. 

I  480 

37 

1770 

'      M 

3.10       " 

127 

19-5 

118    ... 

3h.  25m. 

3870 

45i 

1778 

1      M 

4.50       " 

128 

20.0 

121      

ih.  o6m. 

i  182 

19 

1784 

"     16 

IO.22  A.M. 

128 

ig.O 

115     •••• 

3h.  oSm. 

3642 

40 

1790 

"     16 

1.09   P.M. 

129 

-.c 

log 

ih.  49111. 

2019 

34 

1796 

"      16 

3-12      " 

129 

17.0 

103 

3h.  52m. 

4  169 

172 

1803 

"      If) 

5.02      " 

130 

20.0 

121 

26m. 

443 

60 

1809 

"      17 

9.31   A.M. 

130 

20.0 

121 

ih.  19111. 

I  533 

8 

1810 

'      17 

10.24      " 

130 

20.0 

121 

2h.  I2m. 

2583 

32 

1816 

'      '7 

I.  I  I    P.M. 

131 

18.5 

112 

iSm. 

264 

5« 

1822 

"      I? 

3-15       " 

131 

.'0.1 

121 

2h.  22m. 

2734 

34 

1834 

"      18 

9.31    A.M. 

132 

',.> 

I  ,  ..  , 

3im. 

551 

23 

1835 

"      18 

IO.26       " 

132 

18.0 

109 

ih.  26m. 

I  611 

31 

1840 

"      18 

1.  06       " 

132 

20.0 

121 

4(1.  o6m. 

4  801 

51 

1846 

"     18 

2.06       " 

133 

19.0 

US 

iom. 

203 

9< 

1847 

"      18 

3.20       " 

133 

20. 

124 

ih.  2401. 

i  '623 

s( 

1852 

"      18 

4.21       " 

133 

19. 

118 

2h.  25m. 

2793 

43 

1353 

"      18 

4-59       " 

133 

20.0 

121 

3h.  O3m. 

3  523 

50 

I85S 

"      19 

9.31   A.M. 

133 

20.0 

121 

3h.  55m. 

4<>i3 

65 

I86c 

'      19 

9-45      " 

133 

19. 

118 

4h.  ogrri. 

4863 

78 

1861 

'      19 

9-55     ' 

133 

20. 

121 

4h.  19111. 

5063 

'43 

1  86s 

'      19 

10.44     ' 

'34 

2O. 

121 

iom. 

185 

150 

l86f 

'      19 

10.56     " 

'34 

2O. 

121 

22m 

415 

10; 

186- 

'      19 

11.05     " 

134 

I9. 

118 

3im 

585 

91 

187; 

'      19 

2.08  P.M. 

135 

2O. 

124 

1  3m 

217 

26' 

1878 

'      '9 

3-M     " 

135 

19. 

US 

ih.  nun 

i  547 

It 

i88( 

"      20 

9.30  A.M. 

136 

20. 

121 

3om 

610 

4: 

188- 

"      2O 

IO.2I       " 

136 

20. 

121 

ih.  2im 

I  580 

14-1 

189- 

"       20 

1.03    P.M. 

137 

18. 

109 

;8m 

978 

13- 

i8g< 

"       20 

2.18       " 

137 

18. 

log 

2h.  I3m 

2  318 

ii 

190* 

"       2O 

3.27       " 

138 

16. 

IOO 

3om 

497 

29! 

; 

190. 

"       2O 

4.10       " 

138 

18. 

112 

ih.  13m 

I  277 

ii< 

i36 


WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE   No.   4. — Continued. 
Warren  System. 


I 
a 

z 

Collected. 

Number 
of 
Run. 

Rate  of 
Filtration. 

£ 

73 

a 
J 

Period  of 

Washing. 
Hours  and 
Minutes. 

c 
</5  si 

s.s  . 
s|£ 

u  «  £* 

-JU 

ii. 

3 

u  u. 

o.  w 

a  8 

rt  ^ 

m 

Remarks. 

£| 

11 
u 

l*v 
ogis 

§«* 
I** 

Date. 

Hour. 

1906 
1912 
1916 

1918 
1925 
1926 
1927 
1929 
1934 
1935 
1939 
1940 
1945 
1946 
1951 
1952 
1958 
1961 
1965 
1968 
1972 
1975 
1976 
1977 
1978 

1979 
1980 
1981 
1984 
1985 
198(1 
1987 
1988 
1992 
1997 

2OOO 
2004 
2007 
2OII 
2020 
2030 
2034 
2039 
2042 
2046 
2049 
2053 
2056 
2064 
2075 
2O82 
2098 
2102 
2105 
2IOg 
2IJ2 
2113 
2114 
2115 

2116 

2117 

1896 
Mar.  20 

"         21 
"        21 
"         21 
"         21 
"         21 
"         21 
"         21 
"         23 
'         23 
'         23 
1         23 
'         23 
23 
23 
23 
24 
24 
24 
24 
24 
"         25 
;         25 
'         25 

25 

1       25 

:         25 
'         25 
24-25 
25 
'         25 
"         25 
25 
25 
"         25 
"         25 
'         25 
'         25 
"         25 
"         25-26 
"         26 
"         26 
"         26 
"         26 
"         26 
"         26 
26 
"        26-27 
"        27 
•        27 
27 
27 
27 
'        27 
"        27 
"        28 
"        28 
"        28 
"        28 
"        28 
"        28 

4.46  P.M. 
10.40  A.M. 

11.58     " 

12.51    P.M. 

3'37     " 
4.03     " 
4-33     ' 
5-03     " 
9-37  A.M. 

10.20       " 
II.  IO       " 

11.58    " 

1.  01    P.M. 

2.53     " 
4.27     ' 
5.00     " 
9  A.M.   to  11.30  A.M. 
II.3O      "         "       2.3O  P.M. 
2.30  P.M.    "      5.30     " 
5.30     "        "      8.30     " 
8.30     "        "    11.30     " 
12.21  A.M. 
1.04       " 
I.  14       ' 
1.24       ' 
I  .39       '  ' 
1.54       ' 
2.24       " 
II.3O  P.M.  to  2.30  A.M. 
2.54  A.M. 
3-54     " 

4.12    " 

2.30  A.M.   to     5.30  A.M. 
5.30     "        "      8.30     " 
8.30     "        "    11.30     " 
II.3O      "         "       2.30  P.M. 
2.30  P.M.     "       5.30      " 

5  30    "      "     8.30    " 
8.30    "      "   71.30    " 
11.30     "        "      2.3OA.M. 
2.30  A.M.     "       5.30      " 
5.30      "         "       8.30      " 
8.30      "         "     1I.3O      " 
11.30     "        "      2.30  P.M. 
2.30  P.M.     "       5.30      " 
5-30      "         "       8.30      " 
8.30      "         "     II.3O      " 
11.30     "        "      2.30A.M. 
2.30  A.M.    "      5.30     " 
5.30     "        "      8.30      " 
8.30      "        "    11.30     " 
11.30     "        "      2.30  P.M. 
2.30  P.M.    "      5.30     " 
5.30     "        "      8.30     " 
8.30     "        "    11.30      " 
I2.O3  A.M. 
12.37      " 
12.47      ' 
12.57      " 
1.  12      " 
1.27      " 

I38 
'39 
139 
140 
141 
141 
141 
141 
142 
142 
142 
142 
143 
'43 
144 
144 
M4 
144-145 
145-146 
146 
146-147 
147 
148 
I48 
148 
148 
148 
148 
147-148 
148 
148 
148 
148-149 
149 
150 
150-151 
I5I-I52 
152-153 
153-154 
154-155 
155-156 
156-157 
157-158 
I5S 
159 
1  60 
160-161 
161-162 
162-163 
163 
163-164 
164-165 
165-166 
166-167 
167 
167 
168 
168 
1  68 
1  68 
168 

18.5 
18.5 

18.0 
19.0 
18.0 
19.0 
18.0 
18.0 
15-5 
18.0 
18.0 
18.0 
iS.o 
18.0 
19.5 
18.5 
17-7 

!6.4 
16.3 

19.3 
18.4 
17.0 
17-5 

18.0 
20.  o 

18.5 

18.0 
18.0 
16.4 
18.0 
18.0 
15-0 
15.8 
19.9 
18.2 

17.6 

15-5 

15.6 
17-3 
17-5 
18.  1 
18.3 
17.8 
17-7 
18.4 
18.4 
15.1 
17.6 
18  3 

112 

112 
log 

"5 
109 

115 

109 
109 
94 
109 
109 
109 
109 
109 
118 

112 
107 

99 

99 
U7 
in 
103 
1  06 
109 

121 
112 

log 
log 

99 
log 
109 
91 
96 
120 

no 
103 
94 
114 
95 
105 
1  06 
log 
in 
108 
107 
in 
in 
9i 
107 

ih.  4901. 
ih.  lorn. 
2h.  28m. 
iSm. 
06  m. 
32m. 
ih.  02m. 
ih.  32m. 
O7m. 
5om. 
ih.  4Om. 
2h.  28m. 
I4m. 
2h.  o6m. 
13111. 
46m. 

1877 
i  227 
2647 
266 
97 
507 
1087 
I  597 
138 
828 
i  708 
2558 
183 
2  153 
215 
845 

in 
138 

148 
220 
820 
229 
116 
150 
147 
5i 
60 
60 
440 
5° 
435 
73 
25 

21 
127 

66 
61 
286 
153 
170 
97 
116 
75 
64 
52 
90 
196 
252 
103 
62 
71 
85 

201 

81 

865 

74 

87 

121 
205 
142 
228 

89 

69 

59 
209 
91 
62 
189 
3og 
no 
169 
207 
535 
no 
97 
59 
U5 

C. 
E. 
E. 
E. 
E. 
E. 
E. 

E. 
E. 
E. 

D.   Application  of  chemi 
cals     unsatisfictorv 

3h.  osm. 
lorn. 
2om. 
30111. 
45m. 
ih.  oom. 
ih.  30m. 

3373 
131 
3ii 

481 
75i 
i  071 

i  581 

2h.  oom. 
3h.  oom. 
3h.  i8m. 

2  IOI 
3241 
3491 

on     Run     No.     154; 
chemical   meter  out 
of  order. 

C.   Shut  inlet   12.  03  A.M., 
E.            [outlet  12.  u  A.M. 
E. 
E. 
E. 
E. 

17.8 
17.8 
18.7 
19.4 
17.6 

21.0 

iS.o 
18.0 
iS.o 
18.0 
18.0 

1  08 
108 
"3 
"7 
107 
127 
109 
109 
109 
log 
109 

3h.  4901. 
lorn. 
2om. 
30111. 
45m. 
ih.  oom. 

4050 
124 
324 
504 
784 
I  004 

COMPOSITION  OF  OHIO   RIVER    WATER   AFTER  PURIFICATION. 


«37 


TABLE  No.  4. — Continued. 

Warren  System. 


Serial  Number. 

Collected. 

Number 
Run. 

Ra 

Filti 

leof 

i 

h 
£ 
j 

Period  of 
ServiceSince 
Last 
Washing. 
Hours  and 
Minutes. 

c 
t  c 

K 

K  »2 

:=~U 
b 

!5 

3 

u  w* 
£"s 

S" 

Remarks. 

oi 

•§i 
u 

§  a 

O  u  != 
c<  o 
o  UI 

is.? 

Date. 

Hour. 

2118 
2Iig 
2120 
2123 
2124 
2125 
2126 
2130 
2135 
2138 
2142 
2145 
2154 
2157 
2160 
2164 
2168 
2172 
2181 
2184 
2188 
2191 
2195 
2198 
2202 
2207 
2209 
2215 
2219 
2223 
2228 
2233 
2236 
2241 
2246 
2249 
2254 

2258 
2261 
2266 
2270 
2275 
2280 
2285 

2288 

2293 
2298 
2301 
2309 
2312 
2313 
2314 
2315 
2316 

2317 
2318 
2319 
2321 
2330 
2333 
2336 

1896 
Mar.  28 

"       28 
"       27-28 
"        23 

"     28 

"        28 

28 
"     28 
"    28 

"       28 
"        28 

"     28 

"         28 

"      28-29 
"      29 
29 

"    29 
29 
1     29 
29 

"     29 
1    29-30 
'     30 
1    30 
1     30 
1     30 
30 
31 
1     31 
'    31 

April     i 
I 
"         I 

"            2 
"           2 
2 

3 
3 
3 
4 
4 
4 
6 
6 
6 
7 
7 
7 
8 
8 
8 
8 
8 
8 
8 
8 
8 
8 
8 
9 
9 

1.57  A.M. 
2.27      " 
II.3O  P.M.    to      2.30  A.M. 
3.27  A.M. 

4.27  ; 

4-33     " 
2.30  A.M.   to     5.30  A.M. 

5.30      "        "      8.30      " 
8.30      "        "   11.30      " 
11.30       "        "      2.30    P.M. 
2.30  P.M.     "      5.30       " 
5.30       "        "      8.30       " 
8.30       "         "    11.30       " 

168 
168 
167-168 
168 
1  68 
168 
168-169 
169 
169-170 
170-171 
171 
171-172 
172-173 

18.0 
18.0 
16.8 
18.0 
17-5 
16.0 
17.1 
18.1 
18.4 
19.1 
18.5 
18.3 
18.0 

log 
log 

102 

109 
1  06 
97 
104 
no 
in 
116 
112 
III 
ic.g 

ih.  3om. 
2h.  oom. 

I  494 

2  IO4 

107 
134 
126 
1  60 

221 
2O6 

83 

77 
114 
155 
169 

187 
135 

21 
40 
67 
46 
125 
3OO 
69 

I  So 
52 
92 

E. 
E. 

E. 
E. 
E. 

E. 
Shut     inlet     12.  08     P.M., 
toulet  12.24  P-M- 

C. 
C. 
C. 

3h.  oom. 
4(1.  oom. 
4h.  o6m. 

3184 
4244 

4354 

2.3O  A.M.     "      5.3O       " 
5.30       "        "      8.30       " 
8.30       "         "    11.30       " 
11.30      "       "      2.30  P.M. 
2.3O  P.M.     "      5.3O       " 
5.30       "        "      8.30       " 
8.30       "         "    11.30       " 
11.30      "        "      2.30A.M. 
2.30  A.M.    "      5.30      " 
5.30      "        "      8.30      " 
8.30      "        "  II.3O      " 
II.3O      "        "      2.30  P.M. 
2.30  P.M.    "      5.30      " 
9.35  A.M.    "   11.30  A.M. 
11.30       "        "      2.3O    P.M. 
2.30  P.M.    "      5.30      " 
9.15  A  M.    "   11.30  A.M. 
11.30      "        "     2.30   P.M. 
2.30  P.M.    "      5.30      '  ' 
9.15  A.M.    "   11.30  A.M. 
II.3O      "        "      2.30  P.M. 
2.30  P.M.    "      5.30      " 
9.15  A.M.    "   11.30  A.M. 
I  1.30      "        "      2.30  P.M. 
2.30  P.M.    "     5.30      " 
9.15   A.M.    "   11.30  A.M. 
I  1.30      "        "      2.30   P.M. 
2.30  P.M.    "      5.30      " 
Q.I5  A.M.    "   11.30  A.M. 
11.30      "        "      2.30  P.M. 
2.30  P.M.     "      5.30      " 
9.15  A.M.    "   II.3O  A.M. 
11.30      "        "      2.30  P.M. 
2  30  P.M.      "      5.30       " 
9.  3O  A.M.     "    II.  30  A.M. 
12.10  P.M. 
12.4!)       " 
12.49       " 
12.52       " 
12.55       " 
12.58       ' 
I.I3       " 
1.28       " 
II.3O  A.M.   to    2.30    P.M. 
2.30  P.M.    "      5.30      " 
g.IS  A.M.    "   11.30  A.M. 
11.32  A.M. 

173-174 
174-175 

175 
175-176 
176 
177 
177-178 
178 
178-179 
179 
179-180 
180-181 
181 
182 
182-183 
184-185 
185 
186 
187-188 
188 

188-189 

189-190 
190-191 

191 

192 

193 
193 
194 

'94 
194-195 
195 
195 
195-196 
196 
196 
196 
197 
197 
197 
'97 
197 
'97 
197 
196-197 
197 
197 
'97 

17-3 
17.9 
17-8 
16.2 

18.9 

17-5 
17.2 
17.9 
19.0 
17-3 
17.1 
17-4 
17.9 
17-8 
17.2 
17-5 
17-8 
17.4 
16.6 
17-8 
17.6 
17.4 
18.4 
17.2 
18.0 
17.0 
18.0 
18.2 

lS.2 
16.6 
iS.o 
17.0 
17.0 
18.5 
17.2 
14.0 
18.0 
19.0 
18.5 
18.0 
18.0 
18.0 
18.0 
17-4 
'7-5 
'7-3 
18.0 

105 
1  09 
jo8 
98 
H5 
106 
104 
108 
H5 
104 
103 
105 
1  08 
1  08 
104 
1  06 
108 
105 

101 

1  08 
1  06 
105 
in 
104 
109 
103 
109 
no 

1  10 
101 

log 
103 
103 

112 
104 
85 
log 
U5 

112 

109 

109 
109 
log 
105 
1  06 
104 
109 

M5 
JI3 
"7 
147 
325 
635 
300 

220 
270 
102 
157 
205 
93 
77 
76 
1  80 
87 
81 

25 

37 
39 
37 
25 
59 
51 

124 
91 
127 
117 
93 
81 
33 
53 
37 
70 

I 

1 

8h.  04m. 
03111. 
06  m. 
09  m. 
I2m. 
I5m. 
3om. 
45m. 

8673 

38 
88 
148 
198 
248 
5i8 
778 

7h.  igra. 

7738 

138 


WATER  PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  4. — Continued. 
Warren  System. 


Rate  of 

t 

0 

Collected. 

Filtration. 

h 

i/i  . 

•| 

1 

Number 

a 

Is- 

i 

Period  of 
ServiceSince 
Last 

|IJ 

U  u. 

a 

of 
Run. 

s  • 

6  "  £ 

X 

Washing. 

^1^ 

i>  ~- 

Remarks. 

? 

Date. 

Hour. 

t'a 

c<  o 

Hours  and 
Minutes. 

SsS 

if 

I 

i» 

u 

^  a  cT 

J 

i25 

1" 

iSg6 

2337 

April  g 

11.47  A.M. 

197 

17.0 

103 

7h.  34m. 

8008  126 

2339 

9 

12.02  P.M. 

197 

15.0 

91 

7h.  4gm. 

8  198,  158 

Shut  inlet  11.52  A.M., 

2342 

'  '    g 

II.3O  A.M.  to  2.30  P.M. 

197—198 

18.4 

T  T  T 

7  J 

C.  [outlet  12.08  P.M. 

2345 

198 

l8  .0   Tnn 

126 

C. 

2350 

9 

"    IO 

10.  ig  A.M. 

198 

18.0 

log 

6h.  2401. 

6798 

44 

2352 

"    IO 

10.49   " 

198 

18.0 

109 

6h.  54m. 

7298 

51 

2354 

"    10 

ii.  ig  " 

198 

18.0 

log 

7h.  24m. 

7838 

87 

2355 

"    IO 

9.2O  A.M.  to  II.3O  A.M. 

198 

17  I 

C. 

2357 

"    IO 

11.49  A.M. 

198 

A  /  .  J 

18.0 

log 

7h.  54m. 

8338 

86 

2359 

"    10 

13.31  P.M. 

199 

18.0 

log 

O3m. 

19 

32 

2360 

"    10 

12.34   " 

199 

!8.5 

112 

o6m. 

79 

55 

2361 

"    IO 

12-37   ' 

199 

18.5 

112 

ogm. 

139 

47 

2362 

"    10 

12.40   " 

igg 

18.5 

112 

I2m. 

igg 

29 

2363 

"    10 

12.43   " 

igg 

18.5 

112 

15111. 

259 

39 

2364 

"    IO 

12.58   " 

199 

18.0 

log 

3om. 

519   16 

2365 

"    10 

I.I3   " 

igg 

18.0 

log 

45m. 

789   15 

2366 

"    10 

"    IO 

2.  2O   " 

199 

18.0 

1  7  O 

log 

ih.  52m. 

2  OOgi   23 

C. 

2370 

"    IO 

3.20  P.M. 

199 

1  1  •  y 
18.0 

log 

2h.  52m. 

3  099'  29 

2371 

"    10 

4.2O   " 

igg 

17-5 

1  06 

3h.  5201. 

4  149   30 

2372 

"    10 

5.2O   " 

199 

17.0 

103 

4h.  52m. 

5  229   44 

"    IO 

2.3O  P.M.  to  5.3O  P.M. 

17  7 

C. 

2377 
2379 

"   II 

"   II 

11.30  A.M. 
9.15  A.M.  to  11.30  A.M. 

igg 

IOQ 

1  1  '  1 

18.0 
17.8 

107 
109 
1  08 

7h.  32m. 

8099 

17 
if, 

C. 

2381 

II 

12.  OO  M. 

igg 

18.0 

log 

8h.  02m. 

8629   16 

2383 

"   II 

12.30  P.M. 

199 

18.0 

log 

8h.  32m. 

9119   13 

2385 

"   II 

I.OO   " 

199 

18.0 

log 

gh.  O2m. 

9  709   25 

2387 

"   II 

I.3O   " 

igg 

18.0 

log 

gh.  32m. 

10  159   12 

2396 

"   II 

11.30  A.M.  to  2.30  P.M. 

17.2 

104 

32 

C. 

2400 

"   II 

3-45  P.M. 

200 

16.0 

97 

03m. 

IO 

65 

2401 

"   II 

3.48  " 

200 

18.0 

log 

o6m. 

60 

41 

2402 

II 

3-51  ' 

2OO 

18.0 

109 

ogm. 

120 

62 

2403 

"   II 

3-54  " 

2OO 

18.0 

109 

I2m. 

170   53 

2404 

"   II 

3-57  " 

200 

18.0 

log 

I5m. 

230  37 

2406 

II 

4.12  " 

20O 

18.0 

tog 

3Om. 

500   19 

2407 

"   II 

4.27  ' 

2OO 

18.0 

log 

45m. 

77O   20 

2409 

"   II 

4-57  ' 

20O 

18.0 

log 

ih.  ism. 

1310   ig 

2411 

"   II 

2.30  P.M.  to  5.30  P.M. 

2OO 

17.1 

104 

28 

C. 

2452 

"    20 

10.25  A.M. 

2OI 

26.0 

158 

ih.  23m. 

2  O20   30 

2455 

"    20 

11.58   " 

2OI 

26.0 

158 

.  .  .  .   2h.  56m. 

4400   24 

2458 

20 

2.54  P.M. 

201 

27.0 

164 

•  -  -  -   5h.  52m. 

8  goo   48 

2463 

21 

9.30  A.M. 

202 

22-5 

136 

.  .  .  .      3om. 

622   46 

2465 

"    21 

10.22   " 

2O2 

23.0 

140 

.  .  .  .   ih.  22m. 

I  782   59 

2468 

"    21 

12.35  P.M. 

2O2 

24.0 

146 

3h.  35m. 

4  832   64 

2472 

21 

1.48   ' 

202 

25.0 

152 

....   4h.  48m. 

6  472   96 

» 

2475 

"    21 

2-55   " 

2O2 

24.0 

146 

5h.  55m. 

8  002!  147 

2479 

22 

g.SI  A.M. 

203 

23.0 

140 

5im. 

I  136  104 

2481 

"    22 

10.45   ' 

203 

23.0 

140 

ih.  45m. 

2356  igi 

2484 

"    22 

12.32  P.M. 

2O3 

23.0 

140 

3h.  32m. 

4  7g6  174 

2486 

"    22 

1.22   " 

203 

23-5 

143 

4h.  22m. 

5  gi6  162 

2489 

"    22 

2.56   " 

203 

22.0 

133 

5h.  5&m. 

8  076  ig8 

2495 

"    23 

II.  18  A.M. 

2O4 

23.0 

140 

33m. 

680 

53 

2497 

23 

12.47  !'-M. 

2O4 

24.0 

146 

2h.  O2m. 

2  760   73 

2499 

'    23 

2.00   " 

204 

24.0 

146 

3h.  ism. 

4410'  107 

2502 

!    23 

3  02  " 

204 

24.0 

146 

4h.  1701. 

5  830  167 

2504 

"    23 

4-47  " 

2O4 

24.O 

146 

6h.  O2m. 

8  240 

151 

2508 

24 

9.31  A.M. 

204 

24.0 

146 

yh.  i6m. 

g  920  356 

2510 

24 

"•43  " 

204 

23.0 

140 

gh.  28m. 

12960  375 

2513 

"    24 

I.  Og  P.M. 

2O4 

21-5 

130 

loh.  54m. 

14  830  460 

2516 

24 

2.44   ' 

205 

23.0 

140 

4im. 

882 

220 

2518 

24 

4.41   ' 

205 

23-5 

143 

2h.  38m. 

3572 

330 

COMPOSITION   OF  OHIO   RIVER    WATER  AFTER  PURIFICATION. 
TABLE  No.  4. — Continued. 

Warren  System. 


'39 


1 

£ 
X 

2522 
2524 
2526 
2531 
2534 
2537 
2539 
2543 
2547 
2550 
2556 
2560 
2563 
2588 
2598 
2602 
2607 
2609 
2610 
2611 
2612 
2613 
2614 
2615 
2616 
2617 
2618 
2619 
2620 
2621 
2622 
2623 
2624 
2625 
2626 
2627 
2629 
263: 
2632 
2633 
2634 
2635 
2637 
2639 
2641 
2642 
2643 
2644 
2645 
2646 
2650 
2656 
2659 
2661 
2663 
2670 
2693 
2702 
2712 
2718 
2721 

Collected. 

Number 
of 
Run. 

205 
205 
205 
206 
206-207 
207 
207-208 
209 
209 

210 

Rate  of 

Filtration. 

£ 

•o 

a 

_! 

Period  of 
Service  Sincf 
Last 
Washing. 
Hours  and 
Minutes. 

c 

fc*. 

."•is 

&£& 

•O*  u 

"  "  — 

=  ~u 
£ 

3 

o^- 

!fi 

(8^ 

B 

Remarks. 

si. 

£5 

II 

u 

jk 

CS  = 

§*= 

=  V  - 

s 

Date. 

Hour. 

1896 
April  25 
"      25 
'      25 
'      27 
"      27 
"  27-28 
"      28 
"      28 
"      28 
"  28-29 
"      29 
"      29 
"      29 
"  29-30 
"      3« 
"     30 
"     30 
May     i 
I 
"        I 
"        I 
"        i 
"        I 
"        i 
"        i 
i 
i 
i 
"        i 
"        i 
"       i 
"        i 
"        i 
"        i 
"        i 
"        i 
Apr.  3O-May  I 
May     i 
"        i 
"        i 
i 
"        i 
"        i 
I 
i 
"        i 
"        i 
"        i 
i 
i 
"        i 
"         2 
2 
"          2 
2 

4 
4 
"     4-5 
5 
5 
5 

IO.  15  A.M. 
I2.4O  P.M. 
1.44      " 
9.30  A.M.   to  3.30  P.M. 
3.30  P.M.   "  g.oo    " 

9.30      "        "    3.00A.M. 
3.  00  A.M.     "    g.OO      " 
g.OO      "        "    3.OO  P.M. 
3-OO  P.M.    "    g.OO     " 
9.00      "        "    3.00A.M. 

20.  0 

20.  o 
20.  o 
21.3 

21.2 

20.  6 
22.3 
21.  g 

21.8 

20.5 

121 
121 
121 
12g 

128 
125 

34 
33 
32 
24 

4h.  42m. 
7h.  O7m. 
8h.  ilm. 

6  292 
9172 
10  462 

231 
371 
324 

M3 
5OO 

559 

Application  of  chemicals 
unsatisfactory  on   run 
No.  208  ;   alum   meter 
out  of  order. 

C. 

This  series  of  results  on 
run    No.    215    used    in 
obtaining  the  average 
bacteria  for  this  run, 
but  not  for  the  day. 

Shut  inlet  2.25  P.M.,  out 
let  2.48  r  M. 
From  May  2-9,  inclusive, 
the     results     of     both 
single      samples     and 
those  collected  by  the 
sampler  were  used  to 
obtain      the      average 
bacteria  for  days  and 
for  runs. 

547 
410 
390 
l°57 

9.00    "      "  3.00  P.M. 
3.00  P.M.   "  g.oo    " 
g.oo    "      "  3.00A.M. 
3.  oo  A.M.  "  g.oo    " 
g.oo    "      "  3.00  P.M. 
3.00  P.M.  "  g.oo    " 

12.46  A.M. 

1.58  " 

2.OO     " 
2.02      " 
2.04      " 
2.O6      " 
2.08      " 
2.10      " 
2.12      " 
2.14      " 
2.16      " 
2.18      " 
2.20     " 
2.22      " 
2.24      " 
2.26      " 
2.31      " 
2.41       " 
2.56      " 

2  1  1-2  1  2 
212 
212-213 
213 

21.3 

23.0 
20.3 

20.6 
20.8 

20.  g 

21.  0 

19.  o 
24.0 
20.  o 

2O.O 
2O.  O 
2O.  O 
20.O, 
2O.  O 
21.  0 
2I.O' 
21.  0 
21.  0 
21.  0 
2    .0 
2    .O 
2    .O 
2    .0 
2    .0 

29 
40 
23 
25 
26 
26 
27 

15 
46 
25 
25 
21 
21 
21 
21 
27 

27 
27 
27 
27 
27 

27 

27 
27 
27 

172 
146 
95 
1  20 
76 
go 
193 
187 
243 
170 
199 
123 
144 
144 
71 
64 
57 
86 
145 
85 
94 
IOI 
53 
107 
96 
98 
i") 
45 
53 
87 
IcH 

83 
III 
132 
140 
1  66 
158 
191 
77 
95 
140 
149 
183 
72 
56 
43 
5i 
66 

214 
214 
215 
215 
215 
215 
215 
215 
215 
215 
215 

215 
215 
215 
215 

215 

215 
215 

215 

215 

loh.  34m. 
02m. 
O4m. 
oom. 
oSm. 
lorn. 
I2m. 
14111. 
i6m. 
iSm. 
2om. 
22m. 
24m. 
26m. 
28m. 
3om. 
35m. 
45m. 
ih.  oom. 

13  136 

12 

52 

92 
132 

182 

222 
262 
302 
352 
392 
432 
472 
512 
552 
602 
802 

I  OI2 
I  322 

3.56  A.M. 
4.56      " 
5.56      " 
6.56      " 
-.56      " 
8.56      " 
3.OO  A.M.   to  g.OO  A.M. 
g.  56  A.M. 
10.56    " 

11.56    " 

12.56  P.M. 

1.56      " 
2.43      " 
g.OO      " 

3.45A.M. 
g.oo    " 
12.40  P.M. 
3.00    " 
9.15  A.M.   to  3-OO  P.M. 

3.00  P.M.  "  g.oo    " 
9.00    "      "  3.00A.M. 
3.00  A.M.   "  g.oo    " 
12.31  P.M. 
g.oo  A.M.  to  3.00  P.M. 

215 

215 
215 
215 

215 

215 
215 

215 

215 
215 

215 
215 
215 
216 
217 
217 

217 

217 
217-218 
218-219 
219 

2lg-220 
220 
220 

2    .0 
2    .0 
2    .O 
2    .OJ 
2    .O| 
2    .O 
20.  6 
20.5 
20.5 
2O.O 
21.  0 
21.0 
14-0 
21.5 
21.  0 

27 
27 
27 
27 
27 
27 
25 
24 
24 

21 
27 
27 

85 
30 
27 

2h.  oom. 
3h    oom. 
4h.  oom. 
5h.  oom. 
6h.  oom. 
7h.  oom. 

2432 
3692 
4952 
6  182 
7442 
8662 

8h.  oom. 
gh.  oom. 
loh.  oom. 
nh.  oom. 
I2h.  oom. 
I2h.  47m. 
5h.  44m. 
i8m. 
5h.  33m. 
gh.  I3m. 
Iih.  33m. 

9902 
II  162 
12352 
13652 
14862 
I57I2 
7  188 
364 
6744 
12374 
14244 

21.0 
21  0 
21.7 

20.5 

20.3 
20.  6 
21.  0 
20.5 

127 
127 
131 
124 

122 
124 
127 
124 

7h.  som. 

9769 

140 


WATER  PURIFICATION  AT  LOUISVILLE. 
TABLE  No.  4. —  Continued. 

Warren  System. 


Ra 

teof 

4J 

S 

Collected. 

Filtr 

ation. 

fc 

~ 

.y 

^ 

~  

^>"^~ 

Period  of 

u  *• 

3 

£ 

Number 

o. 

C  0. 

T3 

ServiceSince 

ii--  ^ 

^  ,_• 

e 

3 

of 
Run. 

s« 

^s^ 

£ 

Washing. 

£11 

jLs 

Remarks. 

2 

Date. 

Hour. 

k  3 
'-)   C 

sill 

Hours  and 
Minutes. 

13  4.,-- 

ii 

<$ 

U 

sa" 

J 

£"u 

E 

1896 

2726 

May     5 

2728 
2730 

6 
6 

T2.I5  A.M. 

221 

21  .O 

127 

6h.  55m. 

8  876 

69 

2732 

"       6 

6.OO  A.M. 

222 

21  .O 

127 

52m. 

I  076 

35 

2738 

6 

12.  2O   P.M. 

222 

21  .O 

127 

jh.  I2m. 

8  846 

IOO 

2740            "        6 

3.00       " 

222        20    J 

124 

gh.  52m. 

12  186 

52 

2748                     6 

ooo    227  5O    7 

2751            ''   6-7 

1 

0,6 

2754            "        7 
27571           ''        7 

3.25  A.M. 

223 
224 

22.  0 

27 

33 
26 

urn. 

216 

V" 

IOO 

2758            "       7 

9  OO  A.M. 

224 

21.  0 

27 

5h.  46m. 

7  226 

2762 

7 

3.OO  P.M. 

224 

21.  O 

27 

nh.  4601. 

14790 

30 

2763 

"           7 

g.oo  A.M.  to  3.00  P.M. 

oo 

27 

2770            "       7 

3.OO  P.M.     "    g.OO      '' 

224-225 

' 

*  / 
128 

2771            "        7 
2777              "    7-8 

g.oo  P.M. 

9.OO    P.M.    to  3-OO  A.M. 

225        21.  0 

127 

4h.  3om. 

5836 

51 

2778 

8 

3.OO  A.M. 

225        21.0 

27 

loh.  3001.   13  326 

167 

2783 

"         8 

T  T-2 

2784            "       8 

9-00  A.M. 

226        21.0 

27    4h.  3901.      5674 

1  -*  J 

17 

2789                     8 

g.OO  A.M.    to  3  OO  P.M. 

226       oo  o 

2T 

2790            "       8 
2797            "       8 

3.OO  P.M. 

227      24.0 

227—228 

46    .... 

O5m. 

IOO 

Application  of  chemicals 

2801            "   8-0 

g.OO      "         ''   3.OO  A.M. 

228 

20  '( 

27 

unsa  is  ac  ory  on    run 

2802 
2807 

"       9 
n 

3.OO  A.M. 

228 

2O.5 

124 

0-7 

.  .  .  .       7h.  4im. 

9545 

58 

out  of  order. 

2812 

9 

9.00  A.M. 

229 

20.5 

*•  / 

24 

.  .  .  .      5h.  ogm. 

6482 

43 

2817 

9 

3.00  P.M. 

229 

20.0 

21 

uh.  ogm. 

14322 

49 

Shut  inlet  2.53  P.M.,  out 

2823 

4 

3.OO  P.M. 

230      J2I.O 

27      .... 

6h.  I2m. 

7  958      44 

let  3.13  P.M. 

2829 

' 

g.oo     " 

230        21.  O 

27 

I2h.  I2m. 

15  578      41 

2832 

9.51      " 

•  O2m. 

13      54 

2833 

9-53     " 

231 

21.5 

30      

04m. 

2834 

9-55     ' 

231 

22.  O 

33 

06  m. 

93      88 

2835 

1 

9  57     ' 

231 

22.0 

33 

o8m. 

I33i     71 

2836 

9-59     " 

231 

20.5 

24 

lorn. 

173 

49 

2837 

' 

IO.OI        ' 

231 

21.  O 

127 

I2m. 

213 

49 

2838 

10.03     " 

231 

21.  0 

127 

I4m. 

253 

48 

2S3g[ 

10.04     " 

231 

21.5 

130 

1              I5tn. 

273 

30 

2840 

10.05     " 

231 

22.  O     133 

....              7.6m. 

303 

33 

2841 

10.07     " 

231 

22.0     133 

iSm. 

343 

55 

2842 

10.09     " 

231 

21.5 

130 

2om. 

383 

23 

2843 

1 

10.11       " 

231 

21-5 

130    

22m. 

423 

32 

2844 

" 

10.13     " 

231 

21.  0     127 

....              24111. 

473 

47 

2845 

10.15    " 

231 

21.0 

,   127 

26m. 

513 

25 

284*: 

' 

10.17     " 

231 

2T.O     127 

28m 

553 

33 

2847 

10.19     " 

231 

21.0 

27 

3Otn. 

603 

27 

2848 

10.24     " 

231 

21.0 

27 

35m. 

713 

33 

2849 

10.34    " 

231 

21.  C 

27 

45m 

963 

36 

2850 

10.49    " 

231 

21.  C 

27 

ih.  oom. 

I  243 

27 

2851 

' 

11.49    " 

231 

21.  C 

27 

2h.  oom. 

2483 

76 

2853 

12.49  A.M. 

231 

•Jl  .< 

127    

3h.  oom. 

3733 

48 

2854 

1.49       " 

231 

21.0 

127 

4h.  oom. 

4  973      29 

2855 

" 

2.49       " 

231 

21.  0      127 

5h.  oom. 

6  283      32 

2856 

3.OO       " 

231 

21.  oj  127    ....      5h.  urn 

6443      31 

2859 

' 

3-49     " 

231 

21.0    127 

....       6h.  oom. 

7  503      32 

2860 

1 

4-49     " 

231 

21  .0      127 

7h.  oom 

8713      36 

2861 

' 

5-49     " 

231 

20.  5 

24 

.  .  .  .j     8h.  oom. 

9913      41 

2863 

6.49     " 

231 

20.5 

24 

.  .  .  .  j     gh.  oom. 

II  183      43 

2864 

1 

7-49     " 

231 

21.0 

27 

.  .  .  J   loh.  oom 

12433 

42 

2865 

8.45     " 

231 

21.  0        27 

....     loh.  56m. 

13  683 

73 

2870 

' 

12.  OO  M. 

232 

21.  O 

27 

2h.  nm 

2790 

123 

2878 

8.44  P.M. 

233 

23.0 

40 

lom 

164 

47 

COMPOSITION  OF  OHIO  RIVER    WATER  AFTER  PURIFICATION. 


141 


TABLE  No.  4.— Continued. 
Warren  System. 


Rate  of 

•i 

0 

Collected. 

Filtration. 

£ 

^ 

2 

t 

Number 

S. 

O  O. 

•c 

Period  of 

2-S.j 

U  ^ 

1 

3 
f. 

Date. 

Hour. 

£3 

Pi 

I 

Last 
Washing. 
Hours  and 
Minutes. 

SI! 

t  ~ 

Remarks. 

•S 

2jg 

^  a? 

8 

—  JU 

^CJ 

& 

U 

S 

Z 

m 

1896 

2880 

May  13 

2.0O  A.M. 

233 

21.0 

127 

5h.  26m. 

6534 

44 

2884 

"  13 

8.00  " 

234 

21.0 

127 

3h.  59^- 

4961 

31 

288g     '  13 

1.  00  P.M.            234 

21.0 

127 

8h.  5gm. 

ii  231 

13 

2895)     '  13 

7.00  " 

235 

21.5 

130 

4h.  03m. 

5136 

II 

28gg|     '  14 

3.OO  A.M. 

236 

21.0 

127 

3h.  13111. 

3899 

10 

2904 

1  14 

g.oo  " 

236 

21.  O 

127 

gh.  I3m.  n  38g 

15 

2go8 

'  14 

2.00  P.M. 

237 

22.0 

133 

ih.  47m.  2  330 

18 

2gi2 

"  '4 

S.oo  " 

237 

21.5 

130 

7h.  47m.  9940 

24 

2918 

"  15 

1.  00  A.M. 

238 

21.  O 

127 

5&m.  i  139 

52 

2922 

'  15 

8.00  " 

238 

21-5 

130 

7h.  56m.  g  759 

59 

2g2& 

'  15 

II.  OO   " 

238 

21.5 

130 

loh.  56m.  13  609 

47 

2930 

'  15 

5-og  P.M. 

239 

21.  0 

127 

4h.  56m.  6  250 

14 

2960 

"  15 

11.00   " 

239 

20.  0 

121 

loh.  47m.  13  580 

1  6 

2g6g 

"  16 

5.OO  A.M. 

240 

21.0 

127 

3h.  I3m.  3  162 

25 

2g8o 

"  16 

10  oo  "         240 

22.5 

I36 

8h.  I3m.  9362 

17 

2ggl 

"  16 

3.00  P.M. 

240 

21.0 

127 

I3h.  I3m.  15  652 

4 

2997 

"  18 

12.  OO  M. 

241 

I6.5 

IOO 

0.6 

i6m.    212 

103 

3004 

"  18 

3.05  P.M. 

241 

18.0 

109 

I.O 

3h.  2im.<  3  372 

53 

3007 

"  18 

6.00  " 

241 

16.5 

IOO 

1.2 

6h.  i6m.  6  212 

192 

D. 

3012 

"  18 

g.u  " 

242 

16.0 

97 

0.6 

I5m. 

2IO 

181 

D.  Application  of  chem- 

3°I4 

'  18 

12.  OO   " 

242 

16.5 

IOO 

o.g 

3h.  04m. 

3040 

152 

D.   icals  unsatisfactory 

3017 

'  19 

3-00  A.M. 

242 

16.0 

97 

6h.  0401. 

6  no 

79 

D.   on  runs  Nos.  242 

3020 

'  19 

4-57  " 

243 

16.5 

IOO 

0.6 

osm. 

33 

"7 

D.   and  243;  chemical 

3021 

'  19 

5-07  " 

243 

16.5 

IOO 

0.6 

I5m. 

223 

127 

D.   meter  out  of  order. 

3023 

'  19 

6.00  " 

243 

16.5 

IOO 

0.7 

ih.  o8m. 

I  183 

118 

D. 

3026 

'  19 

8.30  " 

243 

17-5 

1  06 

I.O 

3h.  38m. 

3593 

74 

D. 

3031 

'  19 

12.  OO  M. 

243 

16.5 

IOO 

i.  5 

7h.  o8m. 

7033 

81 

u. 

3034 

'  19 

3.00  P.M. 

243 

16.5 

IOO 

2.0 

loh.  o8m. 

9913 

98 

D. 

3040 

'  19 

6.00   " 

243 

17-5 

1  06 

2.2 

iih.  04m. 

10763 

58 

D. 

3°45 

'  19 

9-°3   " 

244 

16.0 

97 

0-3 

osm. 

88 

log 

3046 

'  19 

9-'3   " 

244 

16.0 

97 

0.6 

I5m. 

238 

185 

3048 

'  19 

12.00   " 

244 

16.5 

IOO 

0.8 

3h.  O2m. 

3018 

41 

3052 

"   20 

3.00A.M.         244 

17-5 

106 

i.  5 

6h.  O2m. 

6038 

40 

3056 

"   20 

6.00  "          244 

18.0 

109 

i.g 

8h.  42m. 

8688 

45 

3059;       '   20 

8.30  "          244 

17-5 

1  06   2.2 

nh.  I2m. 

ii  148 

75 

30681     "  20 

12.00  M.              244 

15-5 

94   2.6 

I4h.  42m. 

14508 

116 

3071!     "  20 

3.00  P.M. 

244 

16.5 

IOO 

3-6 

I7h.  42m. 

17348 

13 

3079:     '  20 

7-35   " 

245 

15-0 

91 

0.7 

osm. 

93 

107 

3080 

"   2O 

7-45  ' 

245 

17.0 

103 

0.6 

ism. 

243 

78 

3081 

"   20 

g.oo  " 

245 

16.5 

700 

0.8 

ih.  3om. 

i  533 

47 

3085 

"   20 

12.00   " 

245 

17-5 

106 

1.2 

4h.  3om. 

4563 

66 

3088 

"   21 

3.00  A.M. 

245 

18.0 

log 

1.4 

7h.  3om. 

7393 

57 

3092 

"   21 

6.00  " 

245 

17.0 

103 

loh.  3om. 

10  263 

49 

3og7 

"   21 

8.30  " 

245 

17-5 

106 

2-7 

I3h.  oom. 

12513 

62 

3103 

"   21 

12.32  P.M. 

246 

16.0 

97 

0.5 

osm. 

n 

in 

3104 

"   21 

12.41  ' 

246 

16.0 

97 

o-5 

iSm. 

161 

20  1 

"   21 

3.00  " 

246 

16.5 

IOO 

2h.  3301. 

2491 

52 

3111 

"   21 

6.00  " 

246 

16.5 

100 

1.  1 

5h.  3301. 

5431 

42 

3"4 

"   21 

g.oo  " 

246 

17.0 

103 

i  .5 

8h.  33m. 

10541 

102 

3120 

"   22 

1.48  A.M. 

247 

15-7 

91 

0.5 

osm. 

97 

52 

3121 

"   22 

1.58   " 

247 

1  -.<> 

109 

0-5 

ISm. 

227 

67 

3122 

"   22 

3.00   " 

247 

17-5 

106 

0.7 

i  h.  1  7m. 

i  227 

17 

3126 

"   22 

6.00  " 

247 

17-5 

106 

I.O 

4h.  I7m. 

4  127 

27 

3i2g 

"   22 

8.30  " 

247 

17.  n 

103 

1-3 

6h.  47m. 

6577 

33 

3136 

"   22 

12.00  M. 

247 

I6.5 

too 

1.6 

loh.  1701. 

10018 

41 

3139 

"   22 

2.50  P.M. 

247 

22.0 

133 

2.O 

I3h.  07m. 

12838 

22 

3144 

"   22 

3-47  " 

248 

16.0 

97 

1  1  .  " 

o8m. 

97 

135 

3145 

"   22 

3-52  " 

248 

16.0  97 

o-5 

I3m. 

177 

f>7 

3M7 

"   22 

6.00  " 

248 

16.0;  97 

0.6 

2h.  2im. 

2237 

36 

3150 

"   22 

g.oo  " 

248 

17-0,  103 

0.8 

5h.  2im. 

5  267   48 

3154 

"   22 

12.00   " 

248 

16.5  too 

1.2 

8h.  2im. 

8  127   52 

I42 


WATER   PURIFICATION  AT  LOUISVILLE. 

TABLE  No.  4. — Continued. 
Warren  System. 


Ra 

teof 

j 

8 

Collected. 

Flit 

ation. 

£ 

•S 

£ 

jj 

^ 

W  L. 

Period  of 

v.  bi 

y 

ji 

Number 

JL 

!  &  . 

"S 

Service  Since 
Last 

sss 

S  oi 

6 

Date. 

Hour. 

Run. 

s  «• 

ul 

•II 

£ 

Washing. 
Hours  and 
Minutes. 

•fc* 

.2.1 

Remarks. 

£ 

D  ^ 

u 

=  a? 

« 
2 

E"5 

n 

1895 

3157 

May  23 

3-OO  A.M. 

248 

16.0 

97 

1.3 

Ilh.  2im. 

II  017 

44 

3160 

"  23 

6.00   " 

248 

16.5 

IOO 

1-7 

I4h.  2im. 

'3937 

30 

3162 

"  23 

8.30   " 

248 

16.0 

97 

1.9 

l6h.  Sim. 

16257 

24 

3174 

"  25 

I2.OO  M. 

249 

ig.5 

18 

ih.  O2m. 

I  443 

49 

3177 

'  25 

2.OO  P.M. 

249 

19.5 

18 

1.  1 

3h.  O2m. 

3613 

21 

3181 

'  25 

6.OO 

249 

20.0 

21 

2.0 

7h.  02m. 

8463 

39 

3184 

"  25 

8.00  " 

249 

2O.  O 

21 

2.5 

gh.  O2m. 

9743 

35 

3188 

"  25 

I2.OO   " 

249 

2O.  O 

21 

3-5 

I3h.  O2m. 

15  513 

46 

3191 

"  26 

2.00  A.M. 

249 

19-5 

18 

3-9 

15(1.  O2m. 

17833 

35 

3194 

"  26 

4.36   " 

250 

20.  o 

21 

0.6 

05m. 

107 

46 

3195 

"  26 

4.46   " 

250 

20.  o 

21 

0.7 

I5m. 

357 

50 

3197 

"  26 

6.00  " 

250 

20.  O 

21 

o.g 

ih.  2gm. 

I  777 

30 

3202 

"  26 

8.30  " 

250 

20.  O 

21 

3h.  5gm. 

4707 

56 

3208 

"  26 

IO.OO   " 

250 

2O.  O 

21 

2.  2 

5h.  2gm. 

6  557 

31 

3212 

"  26 

2  OO  P.M. 

250 

19-5 

18 

3-0 

gh.  2gm. 

11347 

29 

3215 

"  26 

4.OO   " 

250' 

20.0 

21 

3-7 

Ilh.  2gm. 

13727 

33 

3219 

"  26 

6.O5   " 

251 

I8.5 

12 

0.7 

O5m. 

68 

94 

3220 

"  26 

6.15  " 

251 

ig.o 

15 

0.7 

15111. 

228 

37 

3221 

"  26 

8  oo  " 

251 

19.0 

15 

1.  1 

2h.  oom. 

2288 

41 

3224 

"  26 

10.00   " 

25' 

19.5 

18 

1-5 

4h.  oom. 

4638 

39 

3228 

"  27 

2.OO  A.M. 

251 

19.  o 

15 

2.4 

8h.  oom. 

g  188 

26 

3231 

"  27 

4.OO   " 

251 

19.  o 

15 

3-2 

loh.  oom. 

n  488 

28 

3236 

'  27 

7.30   " 

251 

19.5 

18 

2.O 

I3h.  3om. 

15718 

36 

3240 

"  27 

11-51   ' 

252 

19.5 

18 

0.7 

05  rn. 

37 

gi2 

3243 

"  27 

12.  OI  P.M. 

252 

20.  o 

21 

0.7 

I5m. 

347 

23 

3245 

"  27 

3.00   " 

252 

19.5 

18 

1-5 

3h.  I4m. 

3  727 

19 

3255 

'  27 

6.00  " 

252 

19-5 

18 

2.  I 

6h.  I4m. 

7  2g7 

36 

3258 

'  27 

g.oo  " 

252 

20.  o 

21 

3-° 

gh.  I4m. 

10847 

24 

3264 

"   27 

12.  OO  P.M. 

252 

20.  o 

21 

3-8 

I2h.  I4m. 

14337 

60 

326g 

"  28 

3.og  A.M. 

253 

19.  o 

15 

0.6 

osm. 

54 

63 

3270 

"  28 

3-19  " 

253 

19.5 

18 

0.7 

I5m. 

234 

31 

3272 

"  28 

6.00  " 

253 

19-5 

18 

1.  1 

2h.  56m. 

3374 

45 

3275 

"  28 

7-30  " 

253 

19-5 

18 

1-3 

4h.  26m. 

5094 

go 

3279 

"  28 

10.00   " 

253 

19-5 

18 

1.6 

6h.  5&m. 

8  174 

62 

3294 

'•  28 

2.32  P.M. 

254 

20.  o 

21 

0.7 

I5m. 

67 

247 

D.* 

32g5 

"  28 

2.32   " 

254 

20.  o 

21 

0.7 

I5m. 

77 

207 

B.*  Collected  from  weir 

82g6 

"  28 

2.42   " 

254 

20.0 

21 

0.7 

25m. 

267 

328 

D.*   box. 

T-")7 

"  28 

4.00   " 

254 

20.0 

21 

0.8 

ih.  43m. 

i  827 

340 

D.* 

3305 

"  28 

8.00  " 

254 

2O.  O 

21 

1  .  3 

5h.  43m. 

6577 

185 

D.* 

3314 

'•  28 

IO.2O   " 

255 

20.  O 

21 

0.7 

2Sm. 

384 

312 

D.* 

3315 
3324 

"  28 
'  29 

12.33  A.M. 
10.50  P.M. 

256 

255 

ig.o 

20.0 

15 
21 

0.6 

0.8 

05111. 
58m. 

45 
974 

570 
680 

D.* 
D.*  Shut  inlet  10.  48P.M., 

3325 

"  29 

12.43  A.M. 

256 

19-5 

18 

0.7 

I5m. 

235 

325 

[).*    outlet  10.53  P-M- 

3332 

'  2g 

2.OO   " 

256 

19.0 

15 

0.8 

ih.  32m. 

i  735 

220 

D.* 

3343 

'  2g 

4-44  " 

257 

19-5 

18 

0.7 

15m. 

200 

157 

3355 

'  29 

7.30  " 

257 

ig-5 

18 

I.O 

3h.  oim. 

3  520 

88 

3360 

'  29 

12.  OO  M. 

258 

20.0 

21 

0.9 

2h.  3im. 

2950 

89 

3303 

'  29 

2.00  P.M. 

258 

2O.  O 

21 

1.2 

4h.  3im. 

5  3'0 

139 

3367 

'  2g 

6.OO   " 

259 

lg-5 

18 

I.O 

2h.  32in. 

3070 

181 

3373 

1  2g 

8.00   " 

259 

19-5 

18 

1.2 

4h.  32m. 

5490 

80 

3378 

"  2g 

12.OO   " 

260 

19.5 

18 

0.8 

ih.  igm. 

i  505 

293 

5386 

'  30 

2.50  A.M. 

261 

19-5 

18 

0.7 

nm. 

294 

227 

3389 

"  30 

6-55  " 

262 

20.0 

21 

0.8 

1  6m. 

32g 

246 

3399 

:'  30 

IO.IO   " 

262 

19.5 

18 

1.2 

3h.  3im. 

4219 

92 

3402 

"  30 

12.10  P.M. 

263 

2O.  O 

21 

o.g 

O7m. 

112 

93 

3406 

June 

12.  OO  M. 

263 

21.0 

27 

i.g 

6h.  57tn. 

9322 

35 

3408 

3.OO  P.M. 

263 

2O.  O 

21 

2-5. 

gh.  57m. 

II  g52 

64 

3413 

6.00  " 

264 

23.O 

40 

o.g 

3Om. 

666 

31 

3415 

" 

g.oo  " 

264 

23.0 

40 

3h.  3om. 

4806 

50 

3420 

12.  OO   " 

265 

23.0 

40 

I.O 

5gm. 

i  349 

73 

3422 

"    2 

4.00  A.M. 

266 

22.5 

36 

I.O 

35m. 

79° 

in 

Prescribed  amount  of  chemicals  insufficient. 


COMPOSITION  OF  OHIO  RIVER    WATER  AFTER  PURIFICATION. 


143 


TABLE   No.  4. — Continued. 

Warren  System. 


Ra 

,-,,, 

. 

u 

Collected. 

Filtr 

ation. 

S 

c 

O 

It. 

Period  of 

«ti 

'.5 

V 

Number 

6. 

Is.  . 

•a 

ServiceSince 

"  ifi  " 

j 

e 

D 

z 

Date. 

Hour. 

Run. 

ol 

O   S   3 
§?  = 

I 

Last 
Washing. 
Hours  and 
Minutes. 

>  3  " 

fe 

u  <-• 
a 

Remarks. 

•2 

I  i 

=  8.? 

S 

Us 

rt^ 

X 

u 

2 

_] 

u. 

CQ 

1895 

3425 

June  2 

6.45  A.M. 

267 

23.0 

140 

o.g 

ogm. 

260 

e>4 

3428 

"     2 

IO.2O      " 

268 

23.0 

140 

4.0 

ih.  I2m. 

1656 

67 

3431 

"     2 

11.51      " 

269 

24.0 

146 

9-7 

lom. 

1  80 

181 

3435 

"      2 

4.30  P.M. 

271 

23-5 

143 

I.O 

22m. 

568 

121 

3440 

"      2 

6.50      " 

272 

18.0 

109 

0-7 

22m. 

325 

177 

3444 

"      2 

10.47     " 

273 

18.0 

log 

0.7 

27m. 

414 

49 

3446 

"     3 

3.30  A.M. 

274 

17.0 

103 

0.7 

3/m. 

529 

81 

3450 

"     3 

6.00     " 

274 

16.5 

100 

0.9 

3h.  o7m. 

284g 

57 

3453 

"     3 

9.00     " 

275 

16.5 

IOO 

ih.  42m. 

i  797 

77 

3457 

"    3 

12.00     M. 

275 

17-5 

106 

I.O 

4h.  42m. 

4837 

69 

3459 

"    3 

2.00  P.M. 

275 

16.0 

97 

1.2 

6h.  42111. 

6797 

71 

3461 

"     3 

2.58       " 

275 

17.0 

103 

7h.  40111. 

7897 

61 

Shut  inlet  2.42  P.M.,  out 

3462 

"    3 

4-3"     " 

276 

15-5 

94 

0.7 

ih.  oom. 

944 

36 

let  3.00  P.M. 

34<>7 

"     3 

6.00     " 

276 

17.0 

103 

I.O 

2h.  3Om. 

2424 

3471 

"     3 

9.00     " 

276 

17.0 

103 

1.2 

5h.  3om. 

5444 

"38" 

3475 

"    3 

10.50     " 

276 

18.5 

112 

1.2 

7h.  2om. 

7304 

66 

/ 

3477 

"    3 

12.00       " 

277 

16.5 

IOO 

0.5 

osm. 

41 

28 

» 

3480 

"    4 

12.10  A.M. 

277 

17.0 

103 

0.7 

I5m. 

201 

33 

343i 

"     4 

3.OO       " 

277 

16.5 

IOO 

I.O 

3h.  osm. 

3  101 

25 

3486 

"     4 

6.00     " 

277 

16.5 

IOO 

1.2 

6h.  osm. 

5921 

26 

3489 

"     4 

7.00     " 

277 

7h.  O5m. 

6  941 

57 

3491 

"     4 

9.00      " 

278 

I  h.  ogm. 

i  I  ig 

24 

3494 

"     4 

10.35    " 

278 

18.0 

109 

I.O 

2h.  44m. 

2679 

34 

3503 

"     4 

3.52  P.M. 

278 

17.0 

103 

0.7 

8h.  oim. 

8  28g 

36 

3504 

"     4 

5.52       " 

278 

15-5 

94 

2-9 

loh.  oim.' 

10  189 

39 

3508 

"    4 

8-35     " 

279 

20.  o 

121 

o.g 

4&m. 

884 

28 

3534 

"    4 

12.  OO      " 

279 

20.  o 

121 

1-5 

4h.  nm. 

4924 

16 

3538 

"     5 

3.20  A.M. 

280 

19.5 

118 

0.6 

nm. 

201 

43 

3542 

"     5 

6.00      " 

280 

19-5 

118 

I.I 

2h.  5im. 

3251 

33 

3546 

"     5 

g.OO      " 

280 

20.0 

121 

1-5 

5h.  5im. 

6  801 

63 

3553 

"     5 

4.0O  P.M. 

281 

23.0 

140 

1.8 

5h.  33m. 

7521 

87 

3558 

"     5 

IO.OO      " 

282 

23.0 

I4O 

1.8 

5h.  55m- 

6608 

40 

3585 

"     6 

2.27  A.M. 

283 

22.5 

136 

1-5 

3h.  27m. 

4  522 

21 

3591 

"    6 

7.03      " 

283 

23.0 

I4O 

2.1 

8h.  03m. 

10642 

46 

3598 

"     6 

7-57     " 

284 

7-5 

45 

I.I 

O2m. 

15 

31 

3599 

"     6 

i  7.57     " 

284 

O2m. 

15 

84 

3600 

"    6 

7-59     " 

284 

20.  o 

121 

o.S 

04111. 

55 

50 

3601 

"     6 

8.01     ' 

284 

20.  o 

121 

0.8 

o6m. 

95 

34 

3602 

"     6 

8.01     " 

284 

20.  o 

121 

0.8 

o6m. 

95 

3603 

"    6 

8.03     " 

284 

20.0 

121 

0.8 

o8m. 

135 

25 

3604 

"    6 

8.05     " 

284 

2O.  O 

121 

o.g 

lom. 

175 

27 

3606 

"    6 

8.07     " 

284 

25.0 

152 

0.9 

I2m. 

225 

19 

3607 

"     6 

8.09     " 

284 

25.0 

152 

0.9 

I4m. 

275 

14 

3608 

"     6 

8.  II      " 

284 

23.0 

140 

0.9 

l6m. 

320 

16 

3609 

"    6 

8.13     " 

284 

23.0 

140 

o.g 

i8m. 

365 

12 

3610 

"     6 

8.15     " 

284 

25.O 

152 

o.g 

2om. 

415 

9 

3611 

"     6 

8.17     " 

284 

23.0 

140 

o.g 

22m. 

460 

23 

3612 

"     6 

8.19     " 

284 

23.0 

I4O 

o.g 

24m. 

505 

ii 

3613 

"    6 

8.21       " 

284 

22.5 

136 

o.g 

26m. 

550 

8 

3614 

"     6 

8.23     " 

284 

22-5 

136 

o.g 

28m. 

595 

ii 

36i5 

"     6 

8.25     " 

284 

23.0 

140 

o.g 

3om. 

640 

21 

3616 

"    6 

8.27     " 

284 

23.0 

140 

o.g 

32m. 

685 

14 

3617 

"     6 

8.32     " 

284 

22.5 

136 

o.g 

37m. 

795 

16 

3618 

"    6 

8.42     " 

284 

23.O 

140 

o.g 

47m. 

i  025 

16 

3619 

"    6 

8.57     " 

284 

22.0 

133 

I.O 

ih.  O2m. 

i  345 

73 

3622 

"    6 

9-55     ' 

284 

23.0 

I40 

1-3 

2h.  oom. 

2645 

14 

3623 

"    6 

10.55     " 

284 

23.0 

140 

i-5 

3h.  oom. 

3995 

27 

3626 

"    6 

"•55     ' 

284 

23.0 

I4O 

1.8 

4h.  oom. 

5415 

25 

3627 

"    6 

12.55   P.M. 

284 

23.0 

140 

2.O 

5h.  oom. 

6795 

21 

3628 

"     6 

1-55     " 

284 

23-5 

143 

2.  '2 

6h.  oom. 

8  205 

36 

3631 

"    6 

2-55     ' 

284 

23-5 

143 

2.4 

7h.  oom. 

9595 

12 

144 


WATER  PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  4. — Continued. 
Warren  System. 


Rate  of 

J 

u 

Collected. 

Filtration. 

Si 
t 

!/>     . 

15 

jj 

Number 

a 

§s. 

• 

Period  of 
Service  Since 

t.s"  - 

0 

a 

3 

of 
Run. 

"  a 

ls= 

K 

Last 
Washing. 
Hours  and 

!l! 

O.  4; 

Remarks. 

__ 

Date. 

Hour. 

o  c 

8    SB 

'o 

Minutes. 

v  y/£ 

'£  S 

•2 

IS 

'•=  u  „ 

i 

^JCJ 

"U 

$ 

U 

'i 

•3 

£ 

S 

1895 

3634 

June    6 

3.17  P.M. 

284 

20.  O 

121 

7h.  22m. 

10085 

42 

Shut  inlet  3.10  P.M.,  out- 

3656 

9 

12.45    ' 

285 

23.0 

140 

1-3 

3h.  nm. 

3871 

171 

outlet  3.27  P.M. 

3659 

9 

5.00     " 

286 

22.  5 

136 

0.8 

lorn. 

186 

159 

3668 

'        IO 

11.07  A.M. 

286 

22.  O 

133 

1.2 

2h.  43m. 

3656 

50 

3671 

"       10 

I.OO  P.M. 

286 

21-5 

130 

1.6 

4h.  3&m. 

6316 

57 

3675 

"       IO 

3-3°     " 

287 

22.5 

136 

o.g             44m. 

i  015 

40 

3f>8l 

"     II 

10.28  A.M. 

287 

21-5 

130 

1.3 

4h.  I2m. 

5  705 

25 

3684             "      II 

I.OO  P.M. 

287 

22.  ? 

136 

1.8 

6h.  44m. 

9245 

112 

3687|            "      II 

2.15     " 

288 

22.  O 

133 

0.8 

26m. 

499 

16 

3692 

'      II 

3.40       " 

288 

22.  5 

136 

I.O 

ih.  sim. 

2439J     16 

3697 

"       12 

10.18  A.M. 

288 

22.5 

136 

i.. 

4h.  5gm. 

6  729;     27 

3704 

"       12 

2.40  P.M. 

289 

22.5 

136 

o.S 

33m. 

689      53 

3711 

"     '3 

10.11  A.M.                              289 

23.O 

140 

1.  1 

4h.  34m. 

6  219    241 

3718 

'     13 

12.58   I'.M.                            290 

22-5 

136 

I.O 

ih.  4801. 

2417 

log 

3724 

'      13 

2.53      "                               290 

23.0 

140 

l.i 

3h.  43m. 

5087 

48 

373° 

'     13 

5.28     "                         2g'i 

23.O 

140 

0.8 

28m. 

503 

355 

3734 

'      15 

g.oo  A.M. 

67 

B.  From  usual  nlace  * 

3735 

g.oo     '  ' 

216  iK.  From  weir  box.* 

3736            "     15 

g.oo     " 

73     B.  From    filtered  -  water 

3740            "     15 

10.12     "                         2gi 

22.5 

136 

o.g 

ih.  42m.     2  223 

91 

chamber.* 

3743              '     15 

12.20  PrM. 

291 

23.0 

140 

i  .^ 

3h.  som.      5  203 

356 

3747             '      15 

2.58     " 

2g2 

23.0 

140 

o.c 

Som.      i  130 

41 

3753 

'     15 

4-3°     "                         292 

22.0 

133 

i.; 

2h.  22m.      3  240 

42 

3759 

"     16 

IO.22A.M.     ' 

292 

24.0     146 

i  ... 

4h.  44m.     6  560      35 

3766 

-     16 

12.55   P.M.                              293        22.5 

136 

0.8 

24m.        439      31 

3767 

-     16 

3-25       " 

293 

23.O 

140 

1.3 

2h.  54m.     3  969      28 

3772 

"      16 

4-30       " 

293 

23.0 

140 

1.8 

3h.  sgm.     5  479     49 

3776 

"     17 

10.05  A.M.                      2g3 

23.5 

143 

1.8 

6h.  04111.     8449      57 

378o 

"     17 

12.55  P.M.                      2g4 

22.5 

136 

0.8 

32m.        674      Si 

3783 

"     17 

2.51     " 

294 

22.5 

136 

'1.2 

2h.  28m.'    3  454 

89 

3791 

"     17 

4.20     "                         2g4 

23.0 

140 

1.6 

3h.  57m.      54U 

71 

3796 

"     18 

IO.08  A.M.                              295 

23-5 

143 

0.9 

ih.  o8m.      i  439    177 

3801 

"     18 

12.32   I'.M.                               2g5 

23-5 

143 

1.2 

3h.  32m.  '    4399      43 

3809 

"     18 

2-44       "                                  295 

23.0 

140 

i.  7 

5h.  44m.      7  789 

22 

3818 

"     19 

9.58       '                                    296 

22-5 

136 

o.g 

ih.  23m.      i  737      61 

3824 

"      19 

12.40      '' 

296 

4h.  O5m.     4662    in 

Shut  inlet  12.24  P.M.  .out 

j     -» 
3829 

"     19 

2.57       " 

297 

23.0 

140 

I  .  I 

ih.  5001.     2  315      61 

let   12.41   P.M. 

3845 

"      '9 

4.26       "                                  297 

23.0 

140 

I.  ", 

3h.  igm.1    4495      61 

3853 

'     20 

9.26  A.M.                              ?n-7 

4h.  49m.     6999    171 

3856 

"       20 

II.  IO       " 

298 

23.0 

140 

o.g 

36m.         756      77 

3861 

"       2O 

12.38   P.M.                               298 

24.0 

146 

1.  1 

2h.  04m.      2  746 

39 

3862 

"       2O 

12.38       "                                  268 

From       filtered    -  water 

3870 

"      20 

3.22       "                                  298 

23.5 

143 

i.  5 

4h.  48m.     6  536 

77 

chamber. 

3874 

"      20 

4.36       " 

298 

24.0 

146 

1.6 

6h.  02m.     8  256 

65 

[chamber.  f 

3881 

"       22 

9-OO  A.  M. 

690    B.  From   filtered  -  water 

3882 

"       22 

g.oo     " 

78   jB.  From  weir  box.f 

3883 

"       22 

g.oo     " 

145   IB.  From  usual  olace.-r 

3887 
3888 

•'       22 
"       22 

10.08  A.M. 
10.08     " 

299 
o  nn 

2O.5 

124  .. 

ih.  oSm.      i  508 

go 
70 

3893 

"       22 

1.  12  P.M.                      2gg 

23.0 

140    1.4 

4h.  I2m.      5  738 

61 

3894 

"       22 

1.  12       " 

2Q9 

go 

Fi.  From   filtered  -  water 

3898 

"       22 

3.OO       " 

299 

23.5 

143      1.8 

6h.  oom. 

8268 

IO2 

chamber. 

3899 

"       22 

3  .  oo     '  * 

525 

[3.  From   filtered  -  water 

3902 

"       22 

4-5^     " 

299 

23.5 

143 

2.O 

7h.  56m.    10888 

75 

chamber,  [chamber. 

3903 

"       22 

4.56     " 

Q- 

B.  From  filtered  -  water 

3912 

"       23 

10.03  A.M. 

299 

299 

gh.  33m. 

T"!  IlS 

49 

Shut  inlet  10.03  A.M. 

3913 

"       23 

10.05       " 

299 

15-0 

91 

gh.  35m.    13  168 

56 

39M 

'       23 

IO.O7      " 

299 

25.0 

152 

gh.  37m.    13  218 

61 

39r5 

23 

IO.O9      " 

299 

20.0 

121 

gh.  3gm. 

13258 

49 

*  Collected  before  the  filter  was  in  operation,  and  after  period  of  rest  of  39  hours  30  minutes. 
t         "  "         "       "         "     "  "  "        "  39       "       51 


COMPOSITION  OF  OHIO  RIVRR    WATER   AFTKR   PURIFICATION. 


'45 


TABLE  No.  4. — Continued. 

Warren  System. 


Rate  MI 

o3 

S 

Collected. 

Filtration. 

£ 

il  . 

'2 

1 

Number 

,  S.      §1 

•o 

Period  of 
ServiceSinc 

i)L- 

5   . 

s 

7. 

Run. 

8,j 

O  u  = 

X 

Last 

Hoif  ''and 

^>t 

£i 

Remarks. 

Date. 

Hour. 

u  C 

§  ui 

'o 

Minutes. 

£  S3 

S  c 

•E 

'is 

=  ^  ; 

1 

^  J(3 

"u 

« 

u 

S 

J 

£ 

m 

1896 

3gif 

June  23 

IO.  II  A.M. 

299 

20.1 

)     121 

gh.  4im.'  13  298      83 

39n 

"     23 

10.13      " 

299 

2O.  C 

)     121 

gh.  43m.    13338    106 

391? 

"     23 

10.15      " 

299 

2O.  ( 

)     121 

gh.  45m.    13  373 

92 

391? 

'     23 

10.17      ' 

299 

20.  C 

121 

gh.  47m.    1340* 

150 

3920 

"     23 

10.  19     " 

299 

2O.  C 

121 

gh.  4gm.    13438 

72 

3921 

"     23 

10.21        ' 

299 

2O.  C 

121 

.... 

gh.  5im.'  13473 

g2    Shut  outlet  10.22  A.M. 

3924           "     23 

II.O9 

300 

22.= 

136 

o.S               2om.         495 

560 

3926           "     23 

1.25    P.M. 

300 

23-5      '43 

I.  2 

2h.  36m.     3655 

410 

393°           "     23 

3-15       " 

300 

23.0     140 

1.  7!     4h.  26m. 

6  225 

3935            '     23 

5.OO       " 

300 

23.0     140 

1.9 

6h.  nm. 

8738 

'    58" 

3938             '     24 

IO.I4  A.M. 

3OO 

23-5      143 

1.  9 

7h-  55m. 

10895 

132 

3942           "     24 

11.15       " 

300 

8h.  56m. 

12  382 

33O 

Shut  outlet  11.15  A.M. 

3943            '  '     24 

I  1  .  2O       '  ' 

345 

3947            "     24 

12.36       " 

300 
301 

23.0     140 

0.8 

38m. 

713 

275 

chamber. 

3954            "     24 

3-20       " 

301 

23.O     I4O 

1-3 

3h.  22m.     4593 

240 

3904             '     24 

4-45      ' 

301 

23.0     I4O 

1.5      4h.  47m.     6493 

ig5   !                 [outlet  9.54  A.M. 

3977            "     25 

9.40     " 

301 

....      6h.  I2m.     8  393 

Shut     inlet      9.37     A.M., 

3978            "     25 

52     (  B.  From  filtcred-watcr 

4O7g            '  '      in 

O   TO       '  ' 

301 

4081 

"     3° 

V"  J^ 
O.3O       " 

' 

j  I 

4086 

"     30 

11.27    " 

302 

25-5 

155 

0.8 

05  rn. 

57 

37 

4087 

'     3° 

1  1    2O        *  ' 

"     30 

11.32    " 

302 

26.0 

158 

0.8 

lorn. 

217 

51              chamber. 

4089 

"     30 

"-37     ' 

302 

26.O 

I58 

0.8 

1  5m. 

347 

33 

4090 

"     3° 

11.42     " 

302 

23.0 

140 

o.g 

2om. 

497 

21 

4091 

'     3° 

11.47     " 

302 

23.0 

140 

o.g 

25m. 

617 

28 

4<*;2 

"     3° 

11.52     ' 

302 

23.0 

140 

o.g 

3om. 

727 

28 

4"93 

"     3" 

11.57     ' 

302 

23.0 

140 

o.g              35m. 

837 

42 

4094 

11     30 

2.  02    P.M. 

302 

24.0 

146 

o.g 

40111. 

897 

26 

4095 

"     3° 

2.07 

302 

22.0 

I33 

O.  U 

45111 

967 

25 

4096 

"     30 

2.12       " 

302 

23.1 

140 

0.9 

5om. 

1047 

5° 

4097 

"     30 

2.17       " 

302 

23-0 

140 

o.g 

55m. 

I  167 

42 

4098 

"     30 

2.22       " 

302 

23.0 

140 

O.g 

ih.  oom. 

I  307 

29 

4099 

"     30 

2.38       " 

302 

23.0 

140 

O.g 

ih.  i6m. 

I  667 

51 

4104 

"     3° 

2.47       " 

302 

23.0 

140 

1.  1      3h.  2501. 

4657 

62 

4log 

"     30 

4.25       ' 

3°3 

23.O 

140 

37m. 

788; 

40 

4113 

July     I 

IO  22  A.M. 

3«3 

23.0 

140 

1.  1       3h.  o6m. 

4228 

4122 

I 

I.I5    P.M. 

3<>4 

23.0 

I4O 

o.6i             43m. 

934 

4131 

I                         3.17     " 

3"4 

23-5 

M3 

i.i 

2h.  45111. 

3774 

4147                            2                               11.28  A.M. 

306 

23-5 

143 

1  1  m. 

159 

49 

4151 

2                            12.33    P-M. 

306 

24.0 

I46 

o.g      ih.  i6m. 

I  6gg 

130 

4156 

2 

3.03       " 

307 

23.0 

140 

i.o      ih.  28m. 

I  gso 

105 

4164 

3                                  IO.IO  A.M. 

308 

23.0 

140 

1.  1 

2h.  32m. 

3493 

81 

4167 

3                       11.08     " 

308 

23.0 

140    ' 

i.i       3h.  30111 

4823 

57 

4186 

"       3 

1.45    P.M. 

309 

23-5 

'43 

1  .0      ih.  42m. 

3443: 

76 

4196 

3 

3-45      ' 

310 

22.  5 

I36 

0.7'             07m. 

117 

18 

4197 

3 

4-52      ' 

310 

23.0 

140 

0.8      ih.  14111. 

I  607 

167                              [chamber.* 

421  rj 

6 

9-OO  A.M. 

178    B.  From   filtered  •  water 

4203 

6 

g.oo     '  ' 

4204 

6 

g.oo     '  ' 

122    B.  From  weir  box.* 

4216 

"       6 

2.26  P.M. 

311 

21.0 

127 

0.8              osm. 

55 

1  86 

4217 

"       6 

2.31     " 

3" 

22.0 

133 

o.S1             lorn. 

135 

145 

421.S 

6 

2.36     " 

3" 

22.  5 

136 

0.8              15111. 

255 

112 

4219 

6 

2   41        ' 

3" 

22-5 

I36 

0.8              2om. 

355J 

77 

4220 

6 

2.46        " 

3" 

22.5 

I36 

o.S              25m. 

465 

42 

4221 

6 

2.51        " 

311       22.5 

I36 

0.8              3om. 

565 

42 

4222 

"       6 

2.56        " 

311       J22.5 

I36 

0.8              35m. 

705 

40 

4223 

6 

3.01      " 

1 

22.5 

136 

o  .  g             4om  . 

815 

38 

4224 

6 

3-o6     " 

3" 

23.O 

140 

o.g             45m. 

j 

945 

52 

*  Collected  before  the  filter  was  in  operation,  and  after  the  period  of  rest  of  63  hours  and  30  minutes. 


146 


WATER   PURIFICATION  AT  LOUISVILLE. 
TABLE  No.  4. — Continued, 

Warren  System. 


Ra 

teof 

V 

X 

Collected. 

Filtr 

£ 

S 

~ 

. 

t- 

in  u 

Penod  of 

t.  'y 

3 

S 

Number 

6. 

o  a 

"S 

Last 

s^s 

>-  V 

e 

3 

Run. 

—  ~ 

III 

K 

Sly 

«  6 

Remarks. 

.2 

Date. 

Hour. 

3 

.1  L.I 

0 

'Minute^ 

sj! 

S  S 

i 

3 

=  a? 

I 

£"u 

ffl 

1896 

4225 

July  6 

3.II  P.M. 

3" 

23.0 

140 

0.9 

5om. 

io65 

63 

4226 

6 

3.16   " 

3" 

23.0 

140 

I.O 

55m. 

1  185 

46 

4227 

6 

3.21   " 

22.5 

136 

I.O 

ih.  oom. 

1  295 

36 

4228 

6 

3.26   " 

3" 

22.5 

136 

I.O 

ih.  osm. 

1  405 

31 

4230 

6 

3-51  " 

311 

23.0 

140 

1.  1 

ih.  30m. 

2005 

39 

4233 

6 

4.21  ' 

3" 

23.0 

140 

I.I 

2h.  oom. 

2  705 

26 

4240 

6 

5.25  " 

311 

22.0 

133 

1.2 

3h.  04111. 

4175 

54 

4245 

7 

10.00  A.M. 

311 

23.0 

140 

1-4 

4h.  ogm. 

5685 

55 

4252 

7 

I.OO  P.M. 

312 

22.5 

136 

0.8 

iSm. 

303 

112 

4255 

7 

3.00   " 

312 

23-0 

140 

i.i 

2h.  i8m. 

3253 

46 

4259 

7 

5.13   " 

313 

23.0 

140 

0.8 

lom. 

1  60 

114 

4266 

8 

10.55  A.M. 

313 

23.0 

140 

1.  1 

2h.  22m. 

3350 

51 

4267 

8 

12-35  P.M. 

314 

22.  O 

133 

0.8 

o6m. 

88 

118 

4271 

"   8 

3-50  " 

314 

22.0 

'33 

1.  1 

3h.  2im. 

4438 

47 

4274 

"   8 

5.00  " 

315 

22.0 

133 

0.8 

I4m. 

232 

62 

4279 

9 

10.20  A.M. 

315 

22.5 

136 

i  .0 

2h.  04111. 

2  622 

39 

4282 

9 

12.  II  P.M. 

315 

22.0 

133 

1-3 

3h.  55m. 

5  232 

52 

4285 

9 

I.Og   " 

316 

lg-5 

118 

0.7 

osm. 

53 

9 

4286 

9 

I.I4   " 

316 

21.5 

130 

0.7 

lom. 

143 

20 

4287 

9 

I.I9   " 

316 

22.0 

133 

0.8 

I5m. 

263 

55 

4288 

9 

1.24   ' 

316 

22.5 

136 

0.8 

2om. 

373 

51 

4289 

9 

1.29   " 

316 

23-5 

M3 

0.8 

25m. 

483 

74 

4290 

9 

1-34   " 

316 

22.5 

136 

0.8 

3om. 

603 

46 

4291 

9 

1-39  " 

316 

22.5 

136 

0.8 

35m. 

713 

82 

4292 

9 

1.44  ' 

316 

23.0 

140 

0.9 

4001. 

823 

58 

4293 

9 

1.49  " 

316 

22.5 

136 

0.9 

45m. 

943 

39 

4294 

9 

1.54  " 

316 

23.0 

140 

0.9 

5om. 

i  053 

58 

4295 

9 

i-59  " 

316 

23.0 

140 

0.9 

55m. 

i  173 

52 

4296 

9 

2.04  " 

316 

23.0 

140 

I.O 

ih.  oom. 

I  283 

24 

4297 

9 

2.09  " 

316 

23.O 

140 

I.O 

i  h.  osm. 

i  513 

64 

4298 

9 

2.24  " 

316 

23-5 

143 

1.  1 

ih.  2om. 

i  773 

42 

4299 

9 

2-39  " 

316 

23.0 

140 

I.I 

ih.  35m. 

2  113 

33 

4300 

9 

2.54  ' 

316 

23.0 

140 

1.  1 

ih.  som. 

2  553 

37 

4301 

9 

3.09  " 

316 

23.0 

140 

I.I 

2h.  osm. 

2  913 

79 

430ia 

9 

3-24  ' 

316 

23.0 

140 

1.2 

2h.  2om. 

3  163 

45 

4305 

9 

3-39  " 

316 

22.  O 

133 

1.2 

2h.  35m. 

3  513 

40 

4306 
4308 

9 
9 

3.54  ' 
4.09  " 

316 
316 

23.0 

19.  o 

140 

1.2 

2h.  som. 
3h.  O5m. 

3943 
4  183 

75 
M3 

Shut  inlet  4.O7P.M.,  out 

43M 

'  10 

11.07  A.M. 

317 

22.5 

136 

1.2 

2h.  49m. 

3693 

54 

let  4.24  P.M. 

4317 

'  10 

1.  01  P.M. 

317 

22.  O 

133 

1.6 

4h.  43m. 

6283 

137 

4320 

"   10 

3.10   " 

318 

23.O 

140 

I.  I 

ih.  igm. 

I  708 

25 

4323 

"   10 

5-05   " 

318 

24-5 

149 

1-5 

3h.  I4m. 

4378 

69 

4328 

"  ii 

10.31  A.M. 

3I8 

22.5 

136 

1.8 

5h.  lom. 

6988 

41 

4333 

"  ii 

12-59  P-M- 

319 

22-5 

136 

1.  1 

ih.  oim. 

i  469 

36 

4346 

"  ii 

3.12   " 

319 

23.0 

140 

1-5 

3h.  I4m. 

4639 

43 

43^7 

'  13 

IO.IO  A.M. 

320 

22.5 

136 

0.  I 

ih.  lom. 

i  508 

53 

4370 

13 

11.44   " 

320 

23.0 

140 

1.2 

2h.  44m. 

3658 

20 

4375 

'  13 

3.33  P.M. 

321 

23.0 

140 

0.8 

3om. 

639 

42 

4376 

!  '3 

5.08   " 

321 

22-5 

136 

i.i 

2h.  osm. 

2819 

140 

4396 

IQ.lS  A.M. 

321 

23.0 

140 

1.2 

3h.  45m. 
6h.  32m. 

5  139 
8  919 

31 
51 

Shut  outlet  1.05  P.M. 

4409 
4422 

"  M 

3.21   " 

322 

22.0 

133 

I.I 

ih.  54m. 

2538 

17 

4424 

"  J4 

4-55   ' 

322 

23.0 

140 

1-4 

3h.  28m. 

4728 

4442 

"  15 

I.  II   ' 

323 

23.0 

140 

O.g 

35m. 

732 

16 

4443 

'  15 

2.04  " 

323 

23-5 

143 

I.O 

ih.  28m. 

i  972 

37 

4448 

'  IS 

3.12  " 

323 

23.0 

140 

1.2 

2h.  3&m. 

3  562 

37 

4456 

"  16 

9-35  A.M. 

324 

22.5 

136 

O.g 

35m. 

686 

34 

4459 

"  16 

11.04   " 

324 

23.0 

140 

I.  I 

2h.  04111. 

2  756 

15 

4469 

"  16 

I.  II  P.M. 

324 

23.0 

140 

I.  5 

4h.  nm. 

5  726 

4477 

"  16 

2-54   " 

325 

22.5 

136 

0.8 

lom. 

184 

17 

4478 

'  16 

2.59  " 

325 

22.0 

133 

0.8 

I5m. 

273 

32 

COMPOSITION  OF  OHIO  RIVER    WATER   AFTER  PURIFICATION. 


'47 


TABLE  No.  4. — Continued. 

Warren  System. 


Rate  of 

S 

u 

Collected. 

Filtration. 

u 

c 

u 

t/5  . 

£ 

1: 

Number 

I 

!§. 

i 

Period  of 
Service  Sine 
Last 

.  ho 
£  c 

o  u. 

£ 

Run. 

X  „• 

5jjl= 

X 

*lfa 

-  R 

Remarks. 

3 

Date. 

Hour. 

3 

5  — 

jtla 

1 

Minutes. 

jjjl 

P 

X 

u 

i 

-J 

£ 

03 

1896 

. 

4479 

July  16 

3.04  P.M. 

325 

22.  C 

133 

0.8 

2om 

374 

6? 

4480 

"  16 

3.09   " 

325 

22.0 

133 

0.9 

25m 

504 

4 

448  1 

"   16 

3-14   ' 

325 

23.0 

140 

o.g 

3om 

614 

33 

4482 

"   16 

3.19   " 

325 

23.0 

140 

o.g 

35m 

724 

38 

4483 

"  16 

3-24   " 

325 

22.5 

136 

o.g 

4om 

.  844 

30 

4484       '   16 

3.29   " 

325 

22.5 

136 

o.g 

45m. 

954 

59 

4485 

'  16 

3-34  ' 

325 

23-5 

143 

I.O 

5om. 

1074 

40 

4486 

"  16 

3-39  " 

325 

23.0 

140 

I.O 

55m. 

i  184 

18 

4487 

"  16 

3-44  ' 

325 

23.0 

14" 

I.O 

ih.  oom. 

I  304 

27 

4488 

"  16 

3-59  " 

325 

23.0 

140 

i.o   ih.  ism 

1654 

23 

4489 

"  16 

4-14  '           325   23.0  140 

i.i   ih.  3om 

i  994 

ii 

4490 

"   16 

4.29  " 

325 

23.0 

140 

1.  1 

ih.  45m 

2344 

33 

4493 

"  16 

4-44  " 

325 

23.0 

140 

1.2 

2h.  oom 

2694 

17 

4494 

"   16 

4-59  " 

325 

23-0 

140 

1.2 

2h.  1501 

3°54 

15 

4497 

"  16 

5.14  ' 

325 

23.0 

140 

i.' 

2h.  3om. 

3394 

29 

4498 

"   16 

5.29  " 

325 

23.0 

140 

i-3 

2h.  45m. 

3  744 

35 

45°3 

"   '7 

2-37  " 

325 

23-5 

M3 

1-3 

3h.  46m. 

5  124 

ii 

4525 

"  18 

11-37  A.M. 

326 

22.5 

I36 

O.g 

3im. 

708 

23 

4546 

"  18 

1.52  P.M. 

326 

23.O 

140 

1.2 

2h.  46m. 

3728 

2' 

4563 

"  18 

5-12   " 

327 

23-5  M3 

I.I 

ih.  I7m. 

1683 

4570 

"   20 

11.07  A.M. 

327 

22.5  136 

1.4 

3h.  42m. 

4983 

22 

4575 

"   2O 

1.48  P.M. 

328 

23.0  143 

0.8 

i6m. 

305 

5 

4576 

"   20 

3-24   " 

328 

23.0  143 

i.i 

ih.  52m. 

2  515 

21 

458i 

"   20 

5-12   " 

328 

21.5  130 

3-6 

3h.  4om. 

4955 

48 

4603 

"   21 

11.07  A.M. 

328 

23-5  M3 

1.8 

6h.  osm. 

8195 

93 

4608 

"   21 

I.I4  P.M. 

329 

23-5  M3 

I.O 

ih.  nm. 

i  562 

57 

4613 

"   21 

3-19   " 

329 

23.0 

140 

1.4 

3h.  i6m. 

4512 

86 

4616 

"   21 

5-10   " 

330 

22.5 

136 

o.g 

2gm. 

616 

217 

4619 

"   22 

11.02  A.M. 

330   23.0  140 

i.i 

2h.  38m. 

3  626 

383 

4627 

"   22 

3-47  I'-M. 

332   23.0  140 

o.g 

55m. 

i  236 

818 

4633 

"   22 

4.52  " 

332   23.0  140 

1.  1 

2h.  oom. 

2  756 

1055 

4637 

"   23 

II.  l6  A.M. 

333   21.0  127 

o.g 

5om. 

939 

367 

4643 

'   23 

12.54  P.M. 

333   23.0  140 

i.i 

2h.  28m. 

3  I09 

420 

4645 

"   23 

3-°9   " 

334   23.0'  140 

I.O 

44m. 

875 

•  916 

4649 

"   23 

4-59  " 

335 

17.0 

103 

0.8 

I5m. 

143 

685 

4682 

"   24 

1.32  " 

336 

15-5 

94 

0.6 

2om. 

225 

288 

4689 

"   24 

4.20  " 

337 

15-5 

94 

0.7 

[Om. 

101 

900 

4690 

'   24 

4-30  " 

337 

16.0 

97 

0.7 

2om. 

361 

1300 

4691 

"   24 

4.40  " 

337 

[6.0 

97 

0.8 

3om. 

421 

2000 

46913 

"   24 

4.50  " 

337 

Id  M 

97 

0.8 

4Om. 

2500 

4692 

'   24 

5.00  " 

337 

I6.5 

IOO 

o.g 

5om. 

731 

22OO 

4695 

'   24 

5.10  " 

337 

16.0 

97 

o.g 

ih.  oom. 

891 

392 

4696 

'   24 

5-25  " 

337 

15-5 

94 

I.O 

ih.  ism. 

i  131 

1034 

Shutinlet  5.  20  .P.M.,  out 

4/05 

"   25 

11.05  A.M. 

338 

17.0 

103 

ih.  i8m. 

1086 

let  5.30  P.M. 

4710 

"   25 

I.I7  P.M. 

338 

15-0   91 

2.2 

3h.  30m. 

2906 

4l6 

4712 

"   25 

3.15   " 

339 

13-0   79 

2.O 

43m. 

508 

378 

4715 

"  25 

4-43  " 

339 

14.0   85 

4.0 

2h.  Mm. 

i  698 

504 

[chamber.* 

4722 

"  27 

g.oo  A.M. 

I 

B.  From  filtered-water 

4723 

"  27 

g.oo  " 

8 

B.  From  usual  place.* 

4725 

"  27 

9.25  " 

22 

3.  From  filtered-water 

4727 

"  27 

11.49  " 

341 

14.5 

88 

0.8 

39m. 

^33 

26 

chamber. 

4732 

"  27 

2.  II  P.M. 

341 

16.0 

97 

0.7 

3h.  orm. 

2^63 

268 

4733 

"  27 

3-02   " 

341 

19.  o 

"5 

o.g 

3h.  52m. 

3623 

624 

4753 

"  28 

9-45  A.M. 

343 

22.0 

133 

o.g 

I5m. 

226 

61 

4754 

"  28 

9.50   " 

343 

23.5 

M3 

I.O 

2om. 

33° 

394 

4755 

"  28 

9-55  ' 

343 

23-5 

I.O 

2$m. 

446 

113 

4756 

"  28 

IO.OO   " 

343 

23-5 

143 

I.O 

3om. 

566 

36 

4758 

"  28 

10.05  " 

343 

23-5 

143 

I.O 

35m. 

696 

44 

4759 

••  28 

IO.  IO   " 

343 

23.5 

143 

I.O 

4Om. 

816 

53 

4760 

"  28 

10.15  " 

343 

23.O 

140 

I.O 

45m. 

916 

60 

*  Collected  before  the  filter  was  in  operation,  and  after  a  period  of  rest  of  40  hours  and  7  minutes. 


i48 


WATER   PURIFICATION  AT  LOUISVILLE. 
TABLE   No.   4. — Continued. 

Warren   System. 


Rate  of 

j 

a 

Collected. 

Filtration. 

% 

.S 

1 

ai 

Number 

o. 

C   l- 

0  « 

•d 

Period  of 

4J   ^ 

0  u 

3 

Date. 

Hour. 

Run" 

iS 

3  5  5 

I 

Last 

Washing 
Hours  and 
Minutes. 

Sl| 

c 

Remarks. 

1 

u 

i 

J 

£"u 

n 

1896 

761 

July   28 

10.20  A.M. 

343 

23.0 

140 

I.O 

5001. 

1  046 

66 

762 

"       28 

0.25      " 

343 

23.0 

140 

I.O 

55m. 

1  1561    7» 

763 

28 

0.30      " 

343 

23.0 

140 

I.O 

ih.  oom.j     i  266 

77 

765 

"       28 

0-45      " 

343 

23.0    140 

I.O 

ih.  15111. 

i  606 

31 

7"« 

"       28 

I.OO       " 

343 

22.5    136 

1.  1 

ih.  30111. 

1  956    40 

7'") 

"       28 

1.15     " 

343 

22.5    136 

I.O 

ih.  45m. 

2396 

21 

77' 

"       28 

1.30     " 

343 

22.5 

136 

I.I 

2h.  oom. 

2  636 

59 

773 

"       28 

1-45     " 

343 

23.5 

143 

I  .  2        2h.   I5tn. 

2986 

29 

774 

"       28 

2.OO  M. 

343 

23.5 

143 

1  .3      2h.  3om. 

3  336      27 

77' 

"       28 

2.15   P.M. 

343 

23.0    140 

1.3 

2h.  45m. 

36861     53 

\m 

"       28 

2.30      " 

343 

23.0,    140 

1-3 

3h.  oom. 

4  046!     52 

77<) 

"       28 

2-45       " 

343 

23.0 

140 

1-4 

3h.  I5m. 

4  376      61 

1780 

"       28 

I.OO       " 

343 

23.0 

140 

1.4 

3h.  3001. 

4  746      25 

784 

"       28 

J..I5     " 

343 

23.0 

140 

1-4 

3h.  45m. 

5096      31 

17^- 

"       28 

1.30     " 

343 

22.5 

136 

i  .  5 

4h.  oom. 

5  416 

46 

17-7 

"      28 

2.OO       " 

343 

23.O 

140 

1.6 

4h.  3om. 

6146 

14 

17- 

"       28 

2.30       " 

343 

21.0 

127 

i-7 

5h.  oom. 

6826 

18 

17T- 

"       28 

3-OO       " 

343 

21  .O 

127 

i-7 

5h.  3om. 

7476 

33 

1795 

"       28 

5.O2       " 

344 

21-5 

130 

0.9 

1  7m. 

254 

18 

Pi' 

"       29 

II.  10  P.M. 

344 

22.5 

136 

i  .3 

2h.  55m. 

4024 

51 

I.-4I 

29 

1.25       " 

345 

22.0 

133 

1.  1 

ih.  I5m. 

i  601 

90 

r  =  - 

29 

2.56       " 

345 

22.  O|     133 

1-3 

2h.  46111. 

3661 

10 

1862 

29 

5.05       " 

345 

23.O 

140 

1.6 

4)1.  55m. 

6  581 

58 

,«<„ 

1       30 

I.  ig       " 

346 

23-5 

143 

I.O 

37m. 

774 

12 

1S7» 

"       30 

3-43     " 

346 

23-5 

143 

i  .3 

3h.  oim. 

4  134 

15 

4882 

P-7 

'.'.      3I 
1       31 

II.O9  A.M. 
1.58  P.M. 

347 
347 

22.  5 
22.5 

136 
136 

I  .2 
1-7 

2h.  ogm. 
4h.  58m. 

2874      25 
6  764        7 

4893 

"       31 

3-44     ' 

347      23.5 

143 

2.0 

6h.  44m.     9  274!     66 

Jewell  System. 

1895 

2 

Oct.  21 

10.47  A.M. 

, 

25  .  o 

IOI 

76 

''      21 

12^30  P.M. 

2 

S2 

4 

"       21 

3-46    " 

2 

3h.  43m. 

38 

6 

"      22 

9.45  A.M. 

2 

26.0 

105 

4h.  28m. 

6405 

14 

9 

"       22 

11.25     ' 

2 

28.0 

114 

6h.  o8m. 

8465 

42 

'3 

"       22 

1.34  P.M. 

2 

22.  O 

89 

8h.  17111. 

ii  425 

66 

"       22 

1-47      " 

2 

23.5 

95 

Sh.  30111. 

11697!     62    Agitated  surface  of  sand 

15 

"       22                                 3.05       " 

3 

•J-    , 

114 

1  8m. 

504 

84        layer  at  1.39  P.M. 

i? 

"       22 

4.00      " 

3 

28.0 

114 

ih.  1301. 

I  IIO 

49 

20 

"       23 

9.28  A.M. 

3 

3O.O 

122 

2h.  O2m. 

2  782 

no 

22 

'       23 

10.57      " 

3 

30.0 

122      .  .  .  . 

3h.  3im. 

5  319 

55 

24 

"       23 

n.53     " 

3 

29.0 

118 

4h.  27m. 

7088 

53 

26 

"       23 

1.20  P.M. 

3 

29  o 

118 

5h.  54m. 

9496 

56 

28 

"       23 

2.30       " 

3 

28.5 

116 

7h.  0401. 

ii  475 

42 

30 

'       23 

4.17       ' 

3 

29.0 

118 

8h.  5im. 

15  104 

38 

33 

''       23 

5-2O       " 

T 

9h.  54tn. 

16  853 

39 

38 

"       24 

12.12       " 

3 

29.0 

118 

loh.  52m. 

18423 

77 

40 

"       24 

1.30       " 

3 

29.0 

118 

I2h.  lorn. 

20  710 

67 

45 

"       24 

4.06       " 

3 

29.0 

118 

I4h.  46m. 

25097 

52 

47 

'       24 

5.12       i' 

1  5h.  52m. 

27  022 

40 

49 

"       25 

9.53  A.M. 

3 

30.0 

122 

i6h.  32m 

28  105 

34 

51 

'       25 

11.07      " 

3 

29.0 

118 

I7h.  46111 

30324 

24 

53 

'     25 

12.05   P.M. 

3 

26.O 

105 

i8h.  44m.!  31  908 

28 

56 

'      25 

1.32       " 

3 

23.0 

93 

2oh.  iim 

33  948 

27 

58 

"    25 

2.52       " 

4 

30.0 

122 

25m 

786 

28 

59 

•    25 

3-30       " 

4 

3O.O 

122 

ih.  03111 

1971 

36 

63 

"     25 

4.27       ' 

4 

28.0 

114 

2h.  oom 

3638 

29 

65 

"    26 

10.52  A.M. 

4 

20.0 

8l 

4h.  I4m 

7  "5 

10 

68 

"    26 

1.03  P.M. 

5 

2<>  .  < 

105 

i  h.  I3m 

i  951 

32 

7° 

"    26 

4-35       " 

5 

25.0 

IOI 

4h.  4jm 

5785 

12 

COMPOSITION  OF  OHIO  RIVER    WATER  AFTER   PURIFICATION. 

TABLE    No.   4. — Continued. 
Jewell  System. 


149 


1 

E 

z 

1 

72 

78 
80 
92 

9-1 
95 
98 
107 
109 
no 

114 

"7 

IIQ 

123 
125 
127 

129 
147 
148 
152 
156 
170 
171 
"79 
184 
186 
187 
190 
192 
194 
'95 
198 

201 
203 
207 
209 
213 
217 
2  2O 
225 
226 
229 
232 
235 
236 

237 

238 

239 

240 
243 
244 
245 
246 
247 
248 
2513 
2516 
252 
253 
256 
257 

Collected. 

Number 
Run. 

Rate  of 
Filtration. 

£ 
I 
-j 

Period  of 

Service  Since 
Last 
Washing. 
Hours  and 
Minutes. 

""  ti 

fell 
% 
•u>  u 

%-:(j 
X 

'£ 

3  ^ 
P 

Remarks. 

8. 

U.   3 

I* 

u 

Js.  ] 

III 

—  CL  7 

2 

Date. 

Hour. 

1895 

Oct.  28 

"      2g 
"      29 
"      30 
"      30 
"     3° 
"     30 
"     31 
"     31 
"     31 
Nov.     i 

::  • 

2 

::  2 
::  i 

••  \ 

s 

I  ! 

7 
7 

!'.    7 

8 
8 
8 
8 
"       8 
9 
9 
9 
'      II 

"      II 
"      II 

"       12 
"       12 
"       12 
"       12 
"       12 
"        12 
"       13 
'        13 

'     "3 
"     13 
'     13 
'     >3 
"      14 
'      "4 
"      "4 
'      14 
'      15 
'      '5 

10.54  A.M. 
12.05  P.M. 

1-55     " 
3-'7     " 
3.50     " 
4.18     " 
5-25     " 
1.43     " 
2.38     " 
4.16     " 
1.52     " 
4.00    " 
4.3°    " 

II  .02  A.M. 

12.27  I'.M 
1.23      " 

3-27    " 
11.04  A.M. 
11.24      " 
12.54  P.M. 
3-57     " 
IO.5O  A.M. 
11.20     " 
I  .  13  I'.M. 
1.59      " 
2.O9     " 
2.18      " 
2.36      " 
.2.50     " 
3-09      " 
3-32      " 
II  .OO  A.M. 

12.35  r.M. 

I  .  12      " 
2.23      " 
2.46      " 
II  .30  A.M. 

i  .  18  r.M. 

2.27    " 

9.17  A.M. 
9.50      " 
11.06     " 
2.50  P.M. 
10.44  A.M 
1  1  .05     " 
H-35     " 
12.00    M. 
I  .  15  I'.M. 
3.10     " 
g.2O  A.M. 
9.50      " 
10.27      " 
11.27      " 
I.  I  8  P.M. 
2.52      " 
g.02  A.M. 
9.50     " 
12.00    M. 
3.00  I'.M. 
IO.50  A.M. 
12.55  P.M. 

5 

5 
6 
6 
6 
6 
6 
6 
6 
6 
7 
7 
7 
7 
7 
7 
7 
7 
7 
7 
7 
7 
7 
8 
8 
8 
8 
8 
8 
8 
8 
S 
8 
9 
9 
9 
9 
9 
9 
9 
9 
9 
o 

0 
0 

o 

0 

o 

0 

o 

0 

o 

0 

o 
o 

0 

o 
I 

I 
I 

6h.  19111. 
Sh.  39m 
loh.  2901. 

8  916 
10507 

12  776 
772 
1585 
I  998 
2  926 
6527 

7  600 
9061 
ii  790 

600 
i  35i 
4906 

7  3«9 
8846 
10547 
14362 
14874 
17  241 
20  531 
22  002 
22  761 
25432 
59 
334 
549 
I  012 

I  355 
1852 
2439 
4878 
7°77 
7845 
303 
842 
2  534 
5  244 
6863 
8469 
9267 
10772 
15681 
43 
640 
i  411 
2040 
4  212 
6527 

10  308 

10857 
II  764 
13290 
15783 

18  105 
19505 
20482 
23763 
2390 
8  167 
11417 

40 

54 
20 

a 

4 

2 

3 
'3 
16 
16 
ii 
27 
M 
17 
28 
23 
38 
520 
138 
68 
102 
540 
268 
186 
182 
124 
'34 
156 
132 
'33 
178 
192 
222 
193 
107 
226 
128 
128 
'57 
Hoo 
864 

396 
19? 
1356 
178 
308 
283 
260 
244 
106 
136 
106 
104 
74 
140 

172 
116 
82 
68 
92 

Sterilized  filter  on  this  day. 

Agitated    surface    of    sand 
layer  at  2.38  P.M. 

Agitated    surface    of    sand 
layer  at  11.22  A.M. 

Agitated    surface    of    sand 
layer  from  10.42  A.M.  to 
i  .56  P.M. 

Agitated    surface    of    sand 
layer  all  day,  Nov.  n. 

26.0 

21  .O 
24.O 
24.0 
24.O 
27.0 
22.  0 
16.0 
14.0 
21.0 
28.0 
28.0 
32.O 
3O.O 
26.0 
27.0 
27.0 
27.O 
27.0 
28.0 
26.O 
24.O 
22.  O 
26.O 
25.0 

105 
85 
97 
97 
97 
109 
89 
65 
57 
85 
114 
"4 
130 
122 

105 
109 
109 
109 
109 
114 
105 
97 
89 
i°5 
IOI 

02m. 
I2m. 
2im. 
39m. 

53m- 
ih.  I2m. 
ih.  35m. 
2h.  2im. 
3h.  56m. 
4h.  33m. 
1  1  in 
34"i. 
ih.  41111. 
3(1.  2gm. 
4h.  3801. 
5h.  56m. 
6h.  2gm. 
7h.  45<n. 
lib.  29111. 
O2m. 
23m. 

53"i- 
Ih.  i8m. 
2h.  33m. 
4h.  28m. 
6h.  54m. 
7h.  24m. 
8h.  oim. 
gh.  oim. 
loh.  52m. 
izh.  26m. 
i3h.  ism. 
I4h.  03m. 
i6h.  1301. 
ih.  43111. 
5h.  3gm. 
7h.  44111. 

24.0 
24.0 
24.0 
25.0 
27.0 
2O.  O 
21  .O 
25.0 
25.0 
26.0 
29.0 
24.0 
25.0 
24.0 
24.0 
21  .0 
25.0 
25.0 
25.. 
25.0 
25.0 
25.0 
-).' 
24.0 
25.0 
23.0 
20.0 
24-5 

25.0 
24.0 
25.0 
24.0 

23." 

97 
97 
97 

IOI 

109 
81 

85 

IOI 
IOI 

105 

IlS 
97 
IOI 
97 
97 
85 

IOI 
IOI 

IOI 
IOI 
IOI 
IOI 

97 
97 

IOI 

93 
81 

99 

IOI 

97 
IOI 

97 
93 

WATER  PURIFICATION  AT  LOUISVILLE. 

TABLE   No.    4. — Continued. 
Jewell  System. 


Rate  of 

8 

u 

Collected. 

Filtration. 

£ 

.5 

.H 

^ 

-^  — 

"  *  k. 

Period  of 

i.  bi 

•§ 

u 

Number 

a 

o  a 

-o 

Service  Since 

S-s  *j 

^  u 

a 

Run. 

S,j 

ti  5  £ 

X 

Last 
Washing. 
Hours  and 

£g£ 

a  § 

Remarks. 

_ 

Date. 

Hour. 

u  c 

o  K 

'o 

Minutes. 

Ss'ja 

'£  i 

c 

'•§§ 

~  a  cT 

1 

-  JU 

rt  U 

$ 

U 

S 

J 

[i. 

n 

1895 

258 

Nov.  15 

3.29  I'.M. 

II 

22.0 

89 

lOh.  l8m. 

14  961 

86 

"  16 

I  [ 

25.0  101 

18  267 

116 

, 

"  1  6 

•>      M 

1  1 

20  584 

112 

203 

"   16 

32  -3  p  M 

1  1 

146 

204 
267 

"  18 

.  ^  J  i  •  .»»  . 
9.41  A.M. 

1  1 

25  .O  Tnr 

28  137 

276 

268 

"  18 

1  1  .  OO   '  ' 

1  1 

24.0 

Q7 

30  124 

168 

260 

"  18 

12-35  P.M. 

II 

24.  o 

y  / 
97 

32  329 

116 

270 

"  18 

3.O5   " 

II 

25.O 

IOI 

36  138   nS 

27T 

'  '   10 

0.30  A.M. 

1  1 

24.  5 

37  271 

318 

*/  J 

274 

A  V 

IO.  2O   " 

1  1 

24.  o 

99 

07 

38  4°3 

168 

277 

"  20 

12.31  P.M. 

12 

25.0 

y  / 

IOI 

2im. 

412 

3°4 

278 

"   20 

12.51   " 

12 

25.0 

IOI 

4im. 

984 

294 

279 

"   20 

1.05   ' 

12 

25.0 

IOI 

55m. 

i  276 

54 

280 

"   2O 

1  .  2O   " 

12 

25.0 

IOI 

ih.  lom. 

i  714 

68 

281 

"   20 

2.30   " 

12 

25-0 

IOI 

2h.  2om. 

1909 

49 

284 

"   21 

g.22  A.M. 

12 

24.5 

99 

4h.  oim. 

6  117 

142 

285 

"   21 

IO.IO   " 

12 

24.0 

97 

4h.  49m. 

7237 

72 

286 

"   21 

12.03  l'-M. 

12 

25.0 

IOI 

6h.  42m. 

10061 

76 

287 

"   21 

2.OO   " 

12 

25.0 

IOI 

8h.  3gm. 

13072 

50 

290 

"   22 

2.22   " 

12 

24.0 

97 

nh.  o6m. 

16687 

9° 

291 

"   22 

3.32   " 

12 

25.0 

IOI 

I2h.  i6m. 

18487 

36 

294 

"   23 

9-21  A.M. 

12 

26.0 

105 

I2h.  32m. 

I933I 

394 

295 

"   23 

10.24   " 

12 

26.0 

105 

I3h.  35m. 

21  046 

44 

296 

'   23 

I.I5  P.M. 

12 

24.0 

97 

i6h.  i8m. 

24837 

58 

299 

"   23 

3.40   " 

12 

20.0 

81 

iSh.  26m. 

27  4O2 

77 

301 

"  25 

9-45  A.M. 

12 

19-5 

79 

i8h.  43m. 

28  CO2 

378 

305 

'  25 

10.40  " 

12 

20.0 

81 

igh.  38m. 

28  927 

420 

307 

'  25 

11.45  A.M. 

13 

25.0 

IOI 

07111. 

175 

440 

308 

"  25 

n-55  ' 

13 

25-0 

IOI 

17111. 

413 

368 

309 

"   25 

12.05  P.M. 

13 

24.5 

99 

27m. 

622 

364 

310 

"  25 

12.15   " 

'3 

24.0 

97 

37111. 

848 

390 

312 

"  25 

1-35  ' 

13 

24.0 

97 

ih.  57m. 

2605 

366 

314 

"  25 

3-20   " 

13 

26.0 

105 

3h.  42m. 

5356 

484 

320 

"  26 

g.22  A.M. 

13 

27.0 

log 

4h.  oSm. 

6  460 

748 

321 

"  26 

IO.I5   " 

13 

25.0 

101 

5h.  oim. 

7474 

512 

323 

"  26 

11.27   " 

13 

24-0 

97 

6h.  1311. 

9204 

664 

325 

"  26 

1.48  P.M. 

13 

24.0 

97 

Sh  34m.  12  664 

394 

328 

"  26 

3-15   " 

'3 

23.0 

93 

lOh.  oim. 

14633 

386 

331 

"  27 

9.2O  A.M. 

13 

25-0 

IOI 

loh.  3601. 

15  617 

754 

333 

"  27 

IO.I6   " 

13 

26.0 

105 

lib.  32m.  17  078 

875 

337 

"  27 

11.45   " 

13 

25-5 

103 

I3h.  oim 

'9  333 

T358 

339 
342 

'  27 

"   27 

1.33  P.M. 
3.  12   " 

13 
13 

23-5 

95 

I4h.  49m. 
i6h.  28m. 

22  034 
24  259 

972 
704 

345 

"  29 

9.14  A.M. 

13 

25.0 

IOI 

i6h.  48m. 

24  652 

2280 

346 

'  29 

9-45  " 

13 

24.0 

97 

I7h.  igm. 

25407 

665 

Agitated  surface  of  sand 

353 

"  29 

10.51  ' 

13 

21.  O 

85 

i8h.  25m. 

26  945 

343 

layer  from  g.2S  A.M.  to 

355 

"  29  • 

12.01  P.M. 

13 

22.0 

89 

igh.  35m. 

28587 

444 

9.43A.M. 

357 

"   29 

1.47  " 

13 

24-0 

97 

2ih.  2im. 

30880 

328 

362 

"  30 

9.48  A.M. 

14 

24.0 

97 

I2m. 

217 

700 

363 

"  30 

9.58   " 

14 

24.0 

97 

22m. 

511  558 

364 

"  3° 

10.08   ' 

14 

24.0 

97 

32111. 

712  540 

365 

"  30 

IO.I8   " 

M 

24.0 

97 

42m. 

990  528 

366 

"  30 

10.28   " 

14 

24.0 

97 

52m. 

i  233  560 

367 

"  30 

10.38   " 

14 

24-5 

99 

ih.  O2m. 

i  368  546 

369 

"  30 

11.43   " 

14 

26.0 

105 

2h.  07m. 

3112  658 

37i 

"  30 

1.32  P.M. 

14 

24.0 

97 

3h.  56m. 

5  808  834 

375 

Dec.  2 

9.42  A.M. 

14 

25.0 

IOI 

8h.  35m. 

12  2I3;  448 

377 

"   2 

10.43   " 

14 

25.0 

101 

gh.  26m. 

13684:  322 

3  So 

"    2 

12.29  P-M- 

14 

24.0 

97 

nh.  I2m. 

16273;  376 

382 

"    2 

2.32   " 

14 

24.0 

97 

I3h.  ism. 

19  148;  294 

386 

3 

10.31  A.M. 

14 

25.0 

IOI 

I5h.  05m. 

21  901 

392 

COMPOSITION  OF  OHIO  RIVER    WATER   AFTER  PURIFICATION.  151 

TABLE  No.  4. — Contimted. 

Jewell   System. 


Rate  of 

-; 

•> 

Collected. 

Filtration. 

fc 

j£ 

.2 

- 

~"C 

"  S 

Period  of 

!.    M 

"§ 

i 

Number 

a 

S  & 

1 

Service  Since 

"  'J  " 

^  *•" 

s 

Run 

So 

"rt   4J   « 

O   U   3 

X 

Washmfj. 

^Jfc 

S.S 

Remarks. 

z 

Date. 

Hour. 

fc  3 

Hours  and 
Minutes. 

E.  inXl 

I'l 

•c 

Is 

-~  G.  fT 

% 

233 

"u 

« 

u 

7. 

J 

£ 

m 

1895 

388 

Dec.     3 

11.37  A.M. 

14 

24.0 

97 

i6h.  nm. 

23  537    350 

390 

3 

12.55    P.M. 

14 

22.  O 

89 

I7h.  2gm. 

25437    322 

393 

3 

2.15       " 

14 

22.  C 

89 

iSh.  4gm. 

27  206    385 

Agitated  surface  of  sand 

411 

4 

3-07       ' 

14 

25.0 

IOI 

2oh.  O2m. 

29122    372 

layer  at  1.32  P.M. 

414 

4 

4-37     ' 

14 

23.0 

93 

2ih.  32m. 

3i  350 

290 

420 

"       5 

9-47  A.M. 

14 

23.O 

93 

23h.  ogm. 

33716 

264 

422 

5 

10.38     " 

14 

23.0      93 

24h.  oom. 

34  «2g 

150 

425 

5 

11.47    " 

14 

21.01      85 

25h.  ogm. 

36313 

232 

Agitated  surface  of  sand 

427 

"        5 

2.40   P.M. 

15 

24.0 

97 

lom. 

271 

270 

layer  at  12.23  l'-M- 

429 

5 

2.50       " 

15 

24.0 

97 

2om. 

502 

244 

430 

5 

3.OO      " 

15 

25.0 

IOI 

3001. 

761 

192 

431 

"       5 

3.10      " 

15 

26.0 

105 

4Om. 

I  023 

298 

432 

"       5 

3.20      " 

15 

24.0 

97 

5om. 

i  248 

280 

433 

5 

3  30     " 

15 

24.0 

97 

ih.  oom. 

I  482 

368 

436 

5 

3.46     " 

15 

25.0 

IOI 

ih.  i6m. 

i  856 

156 

438 

"       6 

10  04  A.M. 

15 

•Jfj.' 

105 

ih.  43m. 

2  6g2 

240 

442 

"       6 

11.27      " 

15 

24.0 

IOI 

3h    o6m. 

4827 

194 

449 

6 

1.36   P.M. 

15 

24.0 

97 

5h.  ism. 

8  029 

296 

452  |                    6 

3-45     " 

15 

22.0 

89 

7h.  24m. 

ii  206 

236 

453 

7 

9.25  A.M. 

15 

25.0 

IOI 

gh.  29111. 

14  124 

274 

455 

7 

12.24    P.M. 

15 

23.0 

93 

I2h.  28m. 

1  8  442 

124 

458 

7 

12-55       " 

15 

24.0 

97 

I4h.  4gm. 

21438 

864 

Agitated  surface  of  sand 

461 

9 

10.05  A.M. 

15 

22.0 

89 

i8h.  nm. 

26  096 

1  60 

layer  at  2.47  P.M. 

465 

9 

II.I8       " 

15 

22.0 

89 

igh.  22111. 

27655 

144 

467 

"       9 

12.  2O   P.M. 

15 

23.0 

93 

2Oh.  ism. 

28825 

192 

Agitated  surface  of  sand 

468 

9 

I.48       " 

15 

21  .O 

85 

2ih.  43m. 

30  683 

164 

layer  at  11.47  A.M. 

472 

9 

3.38       " 

15 

21.  O 

85 

23h.  26m. 

32836 

172 

Agitated  surface  of  sand 

478 

'       10 

10.40  A.M. 

16 

24.0 

97 

1401. 

592 

224 

layer  at  3.14  P.M. 

479 

"       10 

10.50      " 

16 

24.0 

97 

24m. 

796 

176 

480 

"       10 

11.00       " 

16 

24.0 

97 

34m. 

i  092 

214 

481 

"     10 

II.  10       " 

16 

24.0 

97 

44m. 

i  313 

1  68 

482 

"     10 

1  1.  2O       " 

16 

24.0 

97 

54m. 

i  543 

304 

483 

"       10 

11.30       " 

16 

24.0     97 

ih.  04m. 

I  755 

194 

490 

"     10 

2.07    P.M. 

16 

25.O     IOI 

3h.  4im. 

4498!   268 

494 

"     10 

3-30       " 

16 

24.0     97 

5h.  04m. 

6605    238 

497 

"     ii 

II.O8  A.M. 

16 

28.0    114 

7h.  35m. 

10370 

196 

499 

"     1  1 

12.14   P.M. 

16 

25.0 

IOI 

8h.  4im. 

12  157 

224 

503 

"     ii 

1.24      " 

:6 

25.0 

IOI 

gh.  5im. 

13442 

196 

506 

"     ii 

3-II       ' 

16 

24.0 

97 

nh.  38m. 

16  532 

190 

508 

"       12 

9.36  A.M. 

16 

24.0 

97 

I4h.  i6m. 

20339 

142 

5io 

"       12 

12.00    M. 

16 

23.0 

93 

i6h.  40111. 

23717 

130 

512 

"       12 

3.OO   P.M. 

1  6 

22.0 

89 

igh.  4Om. 

27  717 

176 

Agitated  surface  of  sand 

517 

"     13 

IO.52  A.M. 

16 

24.0 

97 

22h.  4om. 

31  749 

135 

layer  at  4.28  P.M. 

519 

'    13 

1.50    P.M. 

16 

2O.  O 

81 

'26h.  iSm. 

36428 

116 

522 

'    13 

4.44  P.M. 

17 

-'  1  •  " 

97 

3Om. 

530 

127 

524 

'    14 

IO.05  A.M. 

17 

25.0 

IOI 

ih.  42m. 

3001 

103 

526 

'    14 

12.55    P.M. 

17 

21.  0 

85    .... 

4h.  32m. 

7  195 

136 

529 

'      14 

3.08      " 

17 

24.0 

97 

6h.  45m. 

10413 

164 

533 

"      16 

9.25  A.M. 

17 

25.0 

IOI 

gh.  I4m. 

14  128 

148 

535 

"      16 

11.32      " 

17 

25.0 

IOI 

Iih.  2im. 

17  561 

150 

539 

"     16 

2.40  P.M. 

17 

23.0 

93 

I4h.  2gm. 

22  125 

1  86 

5)0 

"     16 

5-15       " 

17 

21.0 

85 

I7h    0401. 

25  508 

go 

544 

"      17 

9.48  A.M. 

17 

2O.  O 

81 

17(1.  2gm. 

93 

545 

"     17 

12.52    P.M. 

18 

2O.  O 

8l 

24m. 

724 

88 

549 

'      17 

3-30       " 

18 

24.0 

97 

3h.  O2m. 

4  501 

148 

550 

"     17 

4.31       ' 

18 

24.0 

97 

4h.  03m. 

6061 

164 

553 

"     18 

9.16  A.M. 

18 

25.0 

IOI 

5h.  07m. 

7684 

168 

555 

"     18 

10.35     " 

18 

24.0 

97 

6h.  26m. 

9650 

168 

557 

"     18 

1.05    P.M. 

18 

22.0 

89 

8h.  5&m. 

13038 

97 

566 

"     18 

3-31       " 

18 

16.0 

65 

uh.  22m. 

15928 

130 

567 

"     18 

4-34     " 

18 

18.0 

73 

I2h.  25m. 

16933 

90 

WATER  PURIFICATION  AT  LOUISVILLE. 

TABLE  No.  4. — Continued. 

Jewell  System. 


Rate  of 

J 

01 

Collected. 

Filtration. 

1 

C 

| 

1 

Number 

R 

I  S. 

i 

Period  of 
Service  Si  nee 
Last 

u  t? 

(J 

s 

of           S   . 

^  s  £ 

X 

Washing. 

^  ™E£ 

S.U 

Remarks. 

1 

Date. 

Hour. 

Run. 

ol 

=<! 

Hours  and 
Minutes. 

1-^ 

rt  8 

•C 

II 

^  a  * 

% 

I=-3^ 

"U 

« 

i 

•J 

n 

1895 

571 

Dec.  19 

9-45  A.M. 

18        18.0      73 

....     13)1.  3om. 

18  114 

116 

Agitated  surface  of  sand 

572 

"     19 

11.48      ' 

18        18.0 

73 

....     I5h.  33m. 

20  187 

53 

layer  at  9.15  A.M. 

573 

'     19 

12.50   P.M. 

19        25.0 

IOI 

•  •  •  .'             lom. 

257 

46 

574 

'      19 

1.  00      " 

19        25.0 

IOI 

.  .  .  .;             2om. 

508 

35 

575 

'      19 

I.IO      " 

19      ,25.0 

IOI 

...              3om. 

646 

45 

576 

'      19 

1.20      " 

19 

25.0    ioi 

....              4om. 

991 

56 

577 

'     19 

1.30      " 

19 

25.01   ioi 

....              5om. 

1331 

71 

578 

'     19 

1.40      " 

19        25.0]   ioi 

....       ih.  oom. 

1499 

93 

579 

'     19 

3-'9      " 

'9 

24.0      g7 

....      2h.  3gm. 

3841 

98 

58i 

'     19 

4.32      ' 

19 

24.0      g7 

3h.  52m 

5  444 

85 

585 

"       20 

g  36  A.M. 

19 

25.0    ioi 

....       5h.  03111. 

7286 

94 

586 

"       20 

IO.OI       " 

19        24.0 

97 

5h.  28m. 

7887 

85 

590 

"       20 

12.  02    P.M. 

19 

24.0 

97 

7h.  2gm. 

10  798 

84 

592 

"       2O 

2.07      " 

19 

24.0 

97 

gh.  34m. 

13628 

144 

595 

"       20 

3-59     " 

19 

20.0 

81 

.  .  .  .     nh.  26m. 

16083 

91 

598 

"       21 

9.26  A.M. 

19        24.0 

97 

I3h.  ism. 

18  234 

124 

Agitated  surface  of  sand 

599 

"       21 

3-57  I'.M. 

20        22.0 

89 

....       2h.  58m. 

4358 

IO2 

layer  at  8.49  A.M. 

604 

"       21 

g.24  A.M. 

20           25.0 

IOI 

....      4h.  40111. 

7010 

Si 

605 

"       21 

10.26     " 

20 

24.0 

97 

5h.  42m. 

8486 

24 

611 

"       21 

12.30    P.M. 

20 

24.0 

97 

....       7h.  46m. 

ii  366 

62 

615 

"       21 

3.28   " 

20 

22.0 

8g 

....     ioh.  44m. 

15400 

1  08 

620 

!  24 

g.3&  A.M. 

2O           23.0 

93 

.  ...     I3h.  o8m.    18  366]     70 

Agitated  surface  of  sand 

626 

24 

12.37    P.M. 

2O               2O.  O 

Si 

....     i6h.  ogm. 

21  980 

92 

layer  at  9.03  A.M. 

630 

'       24 

3.18  •• 

21           24.0 

97 

.  .  .  .'     ih.  42m. 

2319 

7° 

636 

"       26 

IO.O2  A.M. 

21            25.0 

IOI 

i     4h.  45m. 

6  766 

98 

641 

"       26 

12.  IO    P.M. 

21            23.O 

93 

6h.  4im. 

9486 

97 

646 

"      26 

3-59     " 

21 

23.O 

93 

.  .  .  .     ioh.  3001. 

14  799 

468 

652 

"       27 

IO.29  A-M- 

21 

20.0 

81 

....     I3h.  25m. 

18  641 

664 

Agitated  surface  of  sand 

658 

'     27 

1.57    P.M. 

22           24.0 

97 

i8m. 

422 

235 

layer  at  12.02  P.M. 

659 

"    27 

2  26      " 

22 

25.0 

IOI 

47m. 

I   112 

336 

664 

"    27 

3-31       " 

22 

25.0 

IOI 

ih.  52m. 

2737 

346 

670 

•'    27 

4-52       " 

22 

25.0 

IOI 

3h.  I3m. 

4  745 

468 

675 

11    28 

10.02  A.M. 

22 

25.O 

IOI 

4h.  5gm. 

7  312 

855 

681 

"    28 

H.5I       " 

22 

24.O 

97    

6h.  48111. 

9906 

882 

685 

"    28 

3.15    P.M. 

22 

21  .O 

85 

.  ...       gh.  53m. 

I39I4 

702 

Agitated  surface  of  sand 

689 

"    30 

9-54  A.M. 

23 

25.0 

IOI 

1701.        414    126 

layer  at  1.14  P.M. 

690 

"    30 

10.24     " 

23 

23.0 

93 

47m-:    1145    302 

693 

"    30 

1  1  .  09     " 

23 

24.0 

97 

ih.  32m. 

2  igi    880 

(Hp 

"    30 

1.48    P.M. 

23 

25.0 

IOI 

4h.  nm. 

6  020    144 

704 

"    30 

4.48       " 

23 

23.0 

93 

7h.  O2m. 

96(11       102 

Agitated  surface  of  sand 

712 

"    31 

IO.54  A.M. 

24 

25.0 

IOI 

I5m. 

380 

83 

layer  at  4.04  P.M.  and 

715 

"    31 

11.24 

24 

25-5 

IOI 

45»i. 

2035 

55 

Dec.  31,   9.49  A.M. 

719 

"    31 

2.10    P.M. 

24 

24.0 

97 

3h.  3im. 

4934 

560 

Agitated  surface  of  sand 

i8g6 

layer  at  2.38   P.M.  and 

724 

Jan.     2 

9.04  A.M. 

25 

24.0 

97 

22m. 

280 

140 

Jan.  i,  3.  26  to  3.34  P.M. 

725 

"          2 

g.27       " 

25 

25.0 

IOI 

45»i 

825 

152 

733 

"       2 

II    33       ' 

25 

25.0 

IOI 

2h.  47m. 

3  500 

290 

Agitated  surface  of  sand 

73g 

"         2 

2.35    P.M. 

25 

14.0 

57 

5h.  4gm. 

7  280 

560 

layer  at  11.16  A.M. 

742 

"         2 

3-59       " 

26 

25.0 

IOI 

15111. 

273 

184 

744 

"          2 

4.14       ' 

26 

23.0 

93 

3001. 

713 

240 

750 

"       3 

1O.3O  A.M. 

26 

21.0 

85 

3h.  25m. 

4623 

254 

756 

3 

2  05    P.M. 

26 

22.0 

89 

6h.  48111 

8803 

432 

Agitated  surface  of  sand 

761 

4 

10.57  A.M. 

27 

24.0 

97 

i8m. 

425 

364 

layer  at  12.02  p  M. 

764 

4 

11.48       " 

27       23.5]     gs 

ih.  ogm.      i  547 

368 

771 

4 

2  22    P.M. 

27 

20.0 

81 

3h.  43111.     4997 

438 

811 

g 

10.30  A.M. 

28 

25-0 

IOI 

ih.  2om. 

2  OI4 

2IO 

Sterilized  filter  Jan.  8. 

817 

9 

1.5(1    P.M. 

28 

23-5 

95 

4h.  46m.     6  914 

248 

[outlet  11.44  A.M. 

822             '     10 

11.35  A.M. 

28 

I6.5 

67 

ioh.  37m.    14050 

152 

Shut     inlet     11.32    A.M., 

825            "     10 

12.56    I'.M. 

29 

25.0 

IOI 

46111. 

I  OOO 

1  66 

[P.M. 

829           "     10 

1.52       " 

29 

25-0 

IOI 

ih.  42m. 

2  42O 

288 

[from  8.52  A.M.  to  12.  20 

839 

1    ii 

11.35  A.M. 

29 

22.0 

89 

7h.  oim. 

I  705 

152 

Agitated  surface  of  S.L. 

COMPOSITION  OF   OHIO  RIVER    WATER  AFTER   PURIFICATION. 


'53 


TABLE  No.  4. — Continued. 

Jewell  System. 


Rate  of 

.-: 

Collected. 

Filtration.       £ 

in 

•3 

1 

Number 

a 

J  a        -a 

Period  of 
ServiceSince 
I  ast 

w  c 

3 

U     . 

I 

Run. 

SJ  u 

O  S  5     X 

Washing. 

££i 

°~S 

Remarks. 

5 

Date. 

Hour. 

u.  ~ 

Hours  and 
Minutes. 

T:  •*  o 

1  = 

•"- 

!5  — 

~  ^  - 

tn 

~  jj  = 

vfi 

y, 

O 

i 

3 

£ 

a 

1896 

84i 

Jan.  13 

g.59  A.M. 

30        24.0      g? 

1511.          344 

104 

Agitated  surface  of  sand 

842 

'     13 

10.38     ' 

30         25.0     IOI 

54m.      1318 

I76 

layer  from  9.44  A.M.  to 

845 

'      13 

1.58   P.M. 

30        25.0    ioi 

4h.  1401.     6  236 

290 

5.40  P.M. 

848 

"     13 

4.10     "                       30        25.0    ioi 

6h.  26m.     9411 

2O.| 

855       •  14 

11.52  A.M.                     30        23.0;     g3 

loh.  57m.1  15  722 

160 

Agitated  surface  of  sand 

800       '   14 

2.05  P.M.                     30        23.0      93 

13)1.  lom.    18  819 

1  68 

layer  from  8.54  A.M.  to 

866i           "      14 

3.16     " 

30        iig.o      77 

I4h.  2im.    20  36. 

140 

9-57  A.M. 

868'           "     15 

g.4g  A.M. 

31        ,24-0      97 

I5m. 

346 

148 

869)           "      15 

10.  ig     " 

31        24.0      97 

45m. 

987 

116 

872 

'      15 

10.44     " 

31        24.0      97 

ih.  lom.      I  574 

168 

878 

'      15 

12.56  P.M. 

31        24.0      97 

3h.  22m.     4  671 

226 

-  -  -i 

'      15 

3-07     " 

31        24.0      97 

5h.  33m.,    7658 

124 

888 

"     16 

IO.52  A.M. 

31        24.0      97 

gh.  43m.    13626 

I2O 

893 

"      16 

1.05   P.M. 

31        :24.o      97 

nh.  56m.    16  746 

194 

goo 

"      16 

3.05       " 

31        23.0      93 

I3h.  5601. 

ig  626 

230 

Agitated  surface  of  sand 

912 

"      17 

11.23  A.M. 

32        21.0      85 

05m. 

102 

430 

layer     Jan.      17,     10.03 

913 

'     17 

11.28      " 

32        24.0      97 

lom. 

222 

218 

A.M. 

gi6 

'      17 

11.38      " 

32        25.0    ioi 

2om. 

462 

174 

917 

'      17 

11.48      " 

32        23.5      95 

30m. 

672 

240 

918 

'      17 

11.58       " 

32        24.0      97 

4om. 

go2 

292 

921 

'     17 

12  OS   P.M. 

32        23.5      95 

5om. 

i  172 

194 

922 

'      17 

12.18      " 

32        23.5      95 

ih.  oom. 

i  372 

272 

925 

'      17 

1.  06      " 

32        23.0      93 

ih.  48m. 

2532 

290 

930 

'      17 

2.07      " 

32        24.0      97 

2h.  49^. 

3952 

332 

932 

'      '7 

3.00      " 

32        23.0      93 

3h.  42m. 

5  192 

'186 

936 

'      17 

4.00      " 

32       '24.0      97 

4h.  42m. 

6  602 

232 

942 

"      '7 

5.03      " 

32        24.0      97 

5h.  45m. 

8  142 

298 

949 

"     18 

1O.I2  A.M. 

32        23.0      93 

7h.  3gm. 

10  922 

188 

953 

"      18 

i.ig  P.M. 

32       .23.5 

95 

I  oh.  46m. 

15342 

I  So 

960 

"      18 

2.44       " 

32        24.5 

99 

I2h.  nm. 

17342 

igS 

963 

"      20 

g.45  A.M. 

33        22.5      91 

07m. 

1  60 

306 

I'M 

"       20 

IO.OO       " 

33        25.0    ioi 

22m. 

470 

286 

965 

"       20 

10.23     " 

33        24.0      g- 

45"i- 

I  010 

282 

974 

"       20 

4.  18  P.M. 

33        24.0 

97 

6h.  4om. 

9480 

44 

[layer  at  1.39  P.M. 

979 

"       21 

11.32  A.M. 

33        23.0 

93 

loh.  24m. 

14830 

168  Agitated  surface  of  sand 

986 

"       21 

4.20  P.M. 

33       '23.5 

95 

15(1.  I2m. 

21  580 

173  Agitated  surface  of  sand 

<)<)2 

"       22 

9.26  A.M. 

33        23.5 

95 

i6h.  58m. 

24052 

103      layer  at  4.30  P.M. 

<)<)," 

"       22 

2.21    P.M. 

33        23.5 

95 

2ih.  53m. 

3O  7OO 

106 

IK)2 

"       23 

10.  II   A.M. 

34        23.5 

95 

36m. 

824 

88 

008 

"       23 

3.45   P.M. 

34        24.0 

97 

6h.  lom. 

8724 

318 

013 

11      24 

IO.I5  A.M. 

34 

23.5 

95 

gh.  I4m. 

12994 

1  60 

015 

'       24 

1.47  I'-M. 

3-1 

23-5 

95 

I2h.  46m. 

18  027 

124 

022 

"      25 

9.58  A.M. 

34 

23.0 

93 

I7h.  lom. 

24  097 

128  Agitated  surface  of  sand 

025 

'     25 

2.  15   P.M. 

35 

25.0 

IOI 

25m. 

266 

106      layer  at  9.00  A.M.,  and 

034 

'    27 

IO.  IO  A.M. 

35 

25.0 

IOI 

4h.  5im. 

7  186 

688 

from  9.07  A.M.  to  11.32 

1140 

"    27 

1.  09   P.M. 

35 

25.0 

IOI 

~h.  som. 

II  266 

I    196        A.M. 

"45 

"    27 

4'5       " 

35 

23.0 

93 

loh.  52m.    15  426 

952  Agitated  surface  of  sand 

051 

"    28 

g.I5  A.M. 

35 

23.0 

93 

I3h.  lom.'  18  go6 

500 

layer  at  3.10  P.M. 

"54 

"    28 

I.OO  P.M. 

36 

23.0 

93 

ih.  I2m.      I  713 

2  500              [layer  at  3.42  P.M. 

,,'„, 

"       28 

4-35     " 

36 

24.0 

97 

4h.  34m. 

6463 

i  600  Agitated  surface  of  sand 

1,1,1, 

"    29 

IO.  14  A.M. 

36 

23.5 

95 

6h.  oim. 

8583 

3016  Agitated  surface  of  sand 

06g 

"    29 

2.04    P.M. 

37 

23.0 

93 

ih.    24111.       2  02.) 

I  620 

layer  at  11.43  A.M. 

070 

"     2g 

5.04       " 

37 

23-5 

95 

4h.  24m.  i    6  174 

675 

075 

"     30 

11.03  A.M. 

37 

24.0 

97 

7h.  I3m.    10  ig4 

876 

Agitated  surface  of  sand 

077 

"     30 

1.05    P.M. 

37 

23-5 

95 

gh.  ism.    13  094 

780 

layer  at  10.09  A.M. 

,,-.i 

"     30 

2.56       " 

37 

21  .O 

85 

nh.  o6m.    15  534 

804 

084 

"     31 

10.55  A.M. 

38 

24.O 

97 

3h.  3om.'    5  ooi 

811 

Agitated  surface  of  sand 

089 

"     31 

2.36   P.M. 

38 

20.0 

81 

7h.  nm.    10031 

910 

layer  at  11.29  A.M. 

137 

Feb.     5 

IO.22  A.M. 

39 

25.O 

IOI 

27m.        834 

612 

i  |i 

"       5 

11.50      " 

39 

24.0 

97 

ih.  55m.     2924 

468 

M5 

5 

3.08    P.M. 

39        22  ."o 

5h.  ism.j    7534 

600 

'54 


WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  4. — Continued. 

Jewell  System. 


Rate  of 

•i 

£ 

Collected. 

Filtration. 

t 

| 

~ 

1 

Number 

S. 

i  s. 

•0 

Period  of 
ServiceSince 

o  ^ 

u  u- 

1 

X, 

Date. 

Hour. 

of 
Run. 

!l 

•  "  D  ^ 

-<  s 

X 

Last 
Washing. 
Hours  and 
Minutes. 

It 

6 

Remarks. 

« 

3s 

ia" 

J 

£ 

n 

iSg6 

II5<>        Feb.     5 

5.08   I'  M. 

39         22.0 

Sg 

7h.  I3m. 

10  144 

8g2 

1156            "       6 

10.  13   A.M. 

39 

25.0 

IOI 

8h.  04171. 

ii  324 

i  620 

1  1  60            "        6 

12.  14    P   M. 

39        23.5 

95 

.  .  .  . 

ioh.  D5m- 

M  174 

2  1^5 

Agitated  surface  of  sand 

1164            "        6 

3-13        " 

40        24.5 

99 

40111. 

1014 

i  282 

layer  at  1.54  P.M. 

ii6g            "       6 

4.15        ' 

40 

25.0 

IOI 

ih.  42m. 

2  394 

i  196 

1174            "        7 

IO.I8   A.M. 

40 

24.0 

97 

4h.  o8m. 

5814 

238 

[layer  at  11.17  A.M. 

1178            "        7 

1.32    P.M. 

40 

23.0 

93 

7h.  iSm. 

10  3U 

480 

Agitated  surface  of  sand 

1184            "        7 

5.28       " 

41 

23-5 

95 

ih.  2Otn. 

i  814 

i  200 

Agitated  surface  of  sand 

iigo            ••       8 

10  49  A.M. 

4' 

25.0 

IOI 

ih.  43'". 

2  337 

1785 

layer  from  4.08  P.M.  to 

1192 

"       8 

2.  2O    I'.M. 

41 

19.  o 

77 

5h.  Mm. 

6  727 

500 

5.  18  P.M. 

iigfi            "       8 

3.II       " 

41 

22.  O 

89 

6h.  05111 

7827 

i  900 

1204            "       o 

IO.22  A.M. 

42 

25.0 

101 

....              3gm 

go8 

675 

1205                "          0 

1.  01    I'.M. 

42 

22.  O 

89 

....       3h.  14111 

4278 

616 

Agitated  surface  of  sand 

1212                "          0 

3.16       " 

42 

ig.o 

77 

5h.  2gm 

7  138 

516 

layer  at  1  1.47  A.M. 

1217            "       o 

5.02       " 

42 

22.  O 

Sq 

7h.  nm 

9328 

i  155 

Agitated  surface  of  sand 

1222                "          I 

IO.O9  A.M. 

43 

24.5 

99 

24m 

578 

4T5 

layer  at  3.20  P.M. 

1225                "          I 

I2.5O    P.M. 

43 

24.0 

97 

....       3h.  oim 

3978 

735 

Agitated  surface  of  sand 

1228                "          I 

3-13       " 

43 

23.0 

93 

5h.  24m 

7  108 

567 

layer  at  12.40  P.M. 

1232                "       II 

5-12       " 

43 

24.0 

97 

7h.  lom 

9578 

2  365 

Agitated  surface  of  sand 

1241!               "       12 

3-18       " 

45 

18.0 

73 

ih.  4im 

2  2O5 

2  42O 

layer  at  4.00  P.M. 

1242                "       12 

3-40       " 

45 

26.0 

105 

2h.  03m 

2  6g5 

2  360 

1243                "       12 

4-45     ' 

45 

18.5 

75 

.  .  .  .1     3h.  o8m 

4215 

324 

1249                  '       13 

9.48  A.M. 

45 

23.0 

93 

[     4h.  36m 

6  115 

2Og 

1252 

'      13 

12.24    I'-M. 

45 

22.5 

91 

7h.  I2tn 

g  675 

317 

1255 

'     13 

2.18    " 

45 

25.0 

IOI 

gh.  O2m. 

12  igs 

740 

Agitated  surface  of  sand 

I26l 

'      13 

4.50    " 

45 

23.0 

93 

iih.  34m. 

15615 

930 

layer  at  i.oi  P.M. 

1266 

'      M 

10.24  A.M. 

46 

93 

5om. 

I  178      234 

I27O 

I.I7    I'.M. 

46 

23.0 

93 

3h.  38m. 

5013 

I  110 

Agitated  surface  of  sand 

1274 

"      M 

3-19       " 

46 

23-5 

95 

4h-  53m. 

6738 

I  IIO 

layer  at  I2.5g  P.M. 

1278 

"      14 

4.46       " 

46 

24.0 

97 

.  .  .  .|     6h.  2om. 

8818 

940 

1284                "        15 
1288                  '        15 

10.15  A.M. 
1.2g    P.M. 

46 
46 

23.0 
23.0 

93 
93 

....       8h.  igm. 
...  .!   iih.  28m. 

11468      790 
15  688   i  097 

Shut  inlet  2.56  P.M.,  out 

1292                "       15 

3-O2       " 

46 

18.0      73 

....     I3h.  oim. 

I778S!     845 

let  3.09  p.M. 

1297                  '       15 

5.20       " 

47 

24.0 

97 

ih.  46m. 

2  353 

319 

1303                  '17 

IO.  12  A.M. 

47 

24.0      97 

.  .  .  .       3h.  o8m.     4  163 

I  100 

1307                  '17 

I.4U    P.M. 

47 

24.0      g7 

....       oh.  31  m. 

8783 

I  285 

Agitated  surface  of  sand 

I3II                "       17 

3.10        " 

47 

23  -°!      93 

....       8h.  oim. 

10833 

I  362 

layer  at  11.42  A.M. 

1317                "       17 

5.18        " 

48 

25.0 

IOI 

:             i8m. 

394 

5&g 

1321              '      18 

10.27  A   M. 

48 

22.5 

9' 

....       ih.  57m. 

2  7M 

I  885 

1325             "      IS 

II.  5S       " 

'   48 

23.0      93    ....       3h.  26m. 

4  794 

I  250 

1329            "      18 

2.23    P.M. 

48 

22.0      89    ....       sh.  5im. 

7994 

I  645 

Agitated  surface  of  sand 

1332,           "      18 

4-52 

48 

13.0      52 

8h.  2om. 

I  270 

layer  at  1.56  P.M. 

1340              '      18 

5.14       ' 

48 

23.0      93 

....       8h.  42m. 

ii  804 

1855 

1344              '      19 

10.  IS  A.M. 

48 

16.0      65     •••.     ioh.  oim. 

13  4U 

760 

1348              '      19 

n-35     " 

48 

22.  o      89    ....     iih.  i6m. 

15  974 

50 

Agitated  surface  of  sand 

1352 

'     T9 

3.08    P.M. 

49 

22.5 

gi     2om. 

421 

695 

layer  at  11.43  A.M. 

1357 

"      '9 

5.03      " 

49 

26.0    105 

2h.  ism. 

3  on 

2  170 

1363 

'       20 

11.04  A.M. 

49 

24.0 

97 

3h.  05m. 

4151 

28 

1367 

"       20 

I2.O5    I'-M. 

49 

23.0      93     ....      40.  o6m. 

5  591 

88 

1372 

"       2O 

I.  Og       " 

49 

23.°!     93     •  •  •  •       5h.  07111. 

6851 

43  Agitated  surface  of  sand 

1376 

"       20 

2.IO       " 

49 

23.0      93 

....       6h.  o8m. 

8  321 

59 

layer  at  12.46  P.M. 

1378 

"       20 

3  12      " 

49 

24.0 

97 

...  .1     7h.  torn. 

9771 

206 

1381 

"       20                                 4.05       " 

49 

25.0 

IOI 

....       8h.  03m. 

10031 

575 

1385 

"       20 

5.IO       " 

49 

24.0      97 

.  .  .  .j     oh.  o8m. 

12  64! 

i  3go 

1393 

"       21 

II.O4  A.M. 

49 

25.0 

IOI 

....     ioh.  24m. 

14  381 

IO 

1395 
1398 

"       21 
"       21 

12.45    P.M. 

3-og    " 

49 
49 

21.0      85 
23.0       93 

I2h.  osm. 
I4h.  26m. 

16491 
ig  621 

120              [layer  at  1.22  P.M. 
4go  Agitated  surface  of  sand 

1401 

"       21 

4-55       ' 

49 

22-5 

91 

i6h.  I2m. 

22  Oil 

560  Agitated  surface  of  sand 

1409 

"        22 

IO.24  A.M. 

50 

25.01   101     .  .  . 

58m. 

I  331 

65 

layer  at  5.10  P.M. 

1410 

"       22 

1.  08    I'.M. 

50 

21.0       85      ... 

3h.  4201. 

5  071 

715 

[layer  at  1.28  P.M. 

1413 

"        22 

3-05       " 

5" 

24.0 

97 

5h.  46m. 

7781 

i  no  Agitated  surface  of  sand 

COMPOSITION   OF  OHIO   RIVER    WATER  AFTER   PURIFICATION. 


'55 


TABLE   No.   4. — Continued. 

Jewell  System. 


Rate  of 

,- 

0 

Collected. 

Filtration. 

fc 

. 

C 

2 

1 

Number 

£. 

C  £ 

•d 

Service  Since 
Last 

5  ^S 

u  u- 

£ 

a 

of 
Run. 

V     . 

l-': 

I 

Washing. 
Hours  and 

s|£ 

S.S 

Remarks. 

^ 

Date. 

Hour. 

„! 

111 

o 

Minutes. 

lal 

i  = 

'C 

a  33 

~o.S 

d 

—  «  ;j 

£ic_> 

(X 

<_> 

5 

x 

m 

1896 

1416 

Feb.   22 

4.58  P.M.                            50 

23.0      93     7h.  4901. 

10441    700 

1421 

"       24 

10.24  A.M.                            50 

23.0      93     -  -•-       gh.  2501. 

13  225  1  605 

1424 

24 

1.20  I'.M.                            50 

22.  5      91     •  -  -  •     I2h.  2im. 

17235;  404 

1427 

24 

3.26 

5° 

24.5       gg     I4h.  24111. 

20  115        665 

Agitated  surface  of  sand 

1432 

24 

5-19      "                               5" 

23-o      g3    •  •  •  •    l6h.  1701. 

22  844 

6og 

layer  at  2.15  P.M. 

1438 

1       25 

10.30  A.M.                            50 

23.0      93     •  •  •  •     I7h.  58m. 

25  195        960 

1442 

1       25 

I.lS  P.M.                            51 

23.5      95     ••••              i6m. 

335      7«5 

1446 

1       25 

3-12     "                         51 

22.5       91     ....       2h.  10m. 

2965!     610 

1451 

"       25 

5.02       ' 

51 

23-5       95     •  •  •  •       4h.  oom. 

5515      450 

>  157 

"       26 

IO.  2g  A.M. 

51 

25.0    IOI     -.  •  .       5h.  47m. 

7755i     420 

1461 

"       26 

12.  08   P.M. 

51 

23.0      93     •  •  •  •       7h.  26m. 

10  115      295 

1467 

"       26 

3-15     " 

51 

24.5      99    loh.  33111. 

14625      770 

1470 

"       26 

5.18     ' 

51 

20.  5      83     -  •  •  •     I2h.  3&m. 

17495  3  280 

1477 

"       27 

IO.32  A.M. 

51 

24.0      97       -  -  -     I3h.  i6m. 

18415:      igi 

Agitated  surface  of  sand 

I  po 

27 

1.45  I'-M. 

52 

26.0    105     ....              27m. 

670     6g5 

layer  at  9.32  A.M.  and 

1484 

27 

3-02       " 

52 

30.0     112     •  -  •  •       ih.  44m. 

2  8lO 

97° 

12.  18  P.M. 

1489 

27 

5-12       " 

52 

25.5     103     3h.  54m. 

6  430    I  215 

1495 

"       28 

Tn    c      T  o  i 

C.   Sterilized  filter,  Feb. 

1497 

"       28 

10.42  A.M. 

52 

29.5    120    -  -  -  -       5h.  54m. 

9950  i  33° 

28. 

1500 

"       28 

11.50       " 

52 

33-5    136    7h.  02m. 

12050  i  820 

1511 

i  *  •'  . 

C. 

1513 

"       29 

io.3g  A.M. 

53 

53 

*3  •  9 

27.0 

log    .  .  .  .!            4im. 

i  195 

'97 

1517 

29 

1.38    P.M. 

53 

21.5       87     3h.  02111. 

4885 

2  555 

1521 

29 

3-18       " 

53 

27.0    log 

.  .  .  .;     4h.  42m. 

7495   i  910 

1524 

:       29 

3-38       " 

53 

27.0    log    ....       sh.  O2m. 

3  035   2  170 

1527 

29 

5.  II       ' 

53 

27.0    log    ....       6h.  35m. 

10465 

i  175 

1532 

Mar.   2 

9-35  A.M.  to  3.15  P.M. 

Z'l 

i  g&5 

C. 

1533 

"         2 

9.42  A.M. 

DJ 

53 

26.0    105 

.....     7h.  36m. 

12085 

3455 

1537 

"         2 

10.25       ' 

53 

26.0 

105 

....  I     8h.  igm. 

13185  

1541 

2 

1.36  P.M. 

53 

25-5 

103 

nh.  3om. 

18  165  

1545 

"         2 

3-19       " 

53 

25-0 

IOI 

I3h.  I3m. 

20785    I  ?45 

1550 

"         2 

5-10       " 

53 

25.0    loi 

I5h.  03m. 

23  575    I  445 

1553 

"         2-3 

3.l8    P.M.    to  3-2O  P.M. 

C  -7 

t  570  C. 

1558 

"       3 

10.42  A.M. 

J  J 

53 

23.0      g3 

17(1.  i6m. 

26485'     900 

1564 

'       3 

12.58  P.M. 

53 

21  .0 

85 

igh.  22m. 

29515    I  210                [layer  at  2.09  P.M. 

1566 

3 

3-13       " 

53 

22.5 

9' 

2ih.  3im. 

32  395   i  300  Agitated  surface  of  sand 

1568 

"       3"4 

3-2O   I'.M.    to   3-2O   I'.M. 

2?     8 

I  465  C 

1571 

"       3 

5.13   P.M. 

53-54 
53 

43.0 
21-5 

IO4 

85 

23!!.  3im. 

34935   i  885 

1577 

4 

10.48  A.M. 

54 

27-5 

in 

ih.  3om. 

2  393      610 

1581 

'       4 

I.OO  I'.M. 

54 

28.0 

114 

3h.  42111. 

6  0031     880 

1585 

4 

3-20       " 

54 

28.5 

116 

6h.  O2m. 

9853   i  320 

159° 

4 

5  05     " 

54 

28.0 

114 

7h.  47m. 

12783      595 

1596 

5 

IO-39  A.M. 

54 

28.0 

114 

gh.  Sim. 

16253 

885 

|(jOO 

5 

12.53    I'-M. 

54 

27-5 

III 

I2h.  O5m. 

IQ  893 

298 

1603 

"      4~5 

3-2O  P  M.    to  3.20  P.M. 

27.8 

112 

815  r 

1604 

5-6 

3.  2O       '  '       '  '    3.  2O       '  ' 

54 

e  i-C  c 

30.  3 

6  to 

C. 

1605 

"       5 

3.20  P.M. 

3-4     3  j 

54 

28.0 

114 

.  .  .  .     I4h.  32111. 

24013         ')<   = 

1611 

5 

5-14       " 

54 

25.0 

IOI 

.  .  .  .     i6h.  26m. 

27063         725 

1617 

"       6 

10-35  A.M. 

54 

23.0 

93 

i8h.  I7tn. 

29743 

206  Shut     inlet    10.33    A.M., 

1620 

"       6 

II.  17       " 

55 

38-0 

'54 

I8m. 

53''         *' 

outlet  10.41  P.M. 

1622 

"       6 

12.41    P.M. 

55 

'54 

....       ih.  42m. 

3  656         S6 

1626 

"       6 

3.20       " 

55 

36.0 

146 

.  .  .  .  j     4h.  2im. 

9  526       57" 

1627 

6-7 

3.2O  P.M.    to  3-2O  P.M. 

c  r 

28    7 

116 

!  .....  C 

1632 

6 

5.22    I'.M. 

j  j 

55 

*°  .  / 
34-5 

140 

i     f,h.  2301. 

13(06      550 

1638 

"       7 

10.44  A.M. 

55 

25.0 

IOI 

....       Sh.  ism. 

17206;     128 

1642 

7 

12.54  I'-M. 

55 

25.0 

IOI 

loh.  25m. 

2042(1      150 

1647 

7 

3.2O       " 

55 

25.0 

IOI 

I2h.  5im. 

24  046 

197 

1648 

7-9 

3  20  P.M.    to  3.2O  P.M. 

55-56 

23-5 

95 

C. 

1651 

7 

5.19    P.M. 

55 

22-5 

91 

I4h.  5om. 

26  g36      108 

1657 

1      9 

11.00  A.M. 

25.0 

IOI 

ih.  35m 

2  427        5* 

1662 

'       9 

12.52    P.M. 

5f> 

25-5 

103 

3h.  27m. 

5  347        f'i 

WATER  PURIFICATION  AT  LOUISVILLE. 
TABLE  No.  4. — Continued. 

Jewell   System. 


Collected. 

Number 
of 
Run. 

56 
57 
5.6 
56 
57 
57 
57 
57 
57 
57 
57 
57-5S 
57 
58 
53 
58 
58-59 
58 
59 
59 
59 
59 
59 
59 
59-60 
60 
60 
60 
60 
fco 
60 
60 
60-6  1 
61 
61 
61 
61 
61 
61 
61-62 
62 
62 
62 
62 
63 
63 
63 
63 
63 

63 

63 
64 
64 
64 
64 
64 
64 
64 
64-6 
65 
65-6f 

Rate  of 
iltration. 

i 
| 

£ 

i 

2> 

Period  of 
ervice  Since 
Last 
Washing-. 
Hours  and 
Minutes. 

*-   C 

iy 

^JU 

[X. 

3 

5 

.2.8 

|£ 
305 

95 
no! 
82 
in 
58 
166 
295 
79 
'34 
165 
325 
105 
155 
560 
i&5 
37° 
121 
7OO 
742 
325 
420 
230 
32O 
410 
510 
131 
64 
49 
72 
39° 
169 
M7 
98 
188 
261 
161 
156 
128 
95 
8q 
C7 

Remarks. 

c 

i 

Is. 

i  £  j» 

~i<  o 

o  ,_£ 

-  o.  ?f 

2 

a 

7. 

1668 
1669 
1673 
1679 
1683 
1687 
1688 
1694 
1700 
1703 
1707 
1711 
1714 
1720 
1724 
1728 
1729 
173 
174 
'74 
174 

'75 
175 
176 
176 
176 
177 
'77 
177 
177 
178 
1786 
1791 
1792 
1797 
1  79? 
1804 
1811 
iSis 
181- 
l8ii 
182; 

lS2< 

lSj( 

183 
184 

184 
184 
184 
185 

1  86 
1  86 

187 
187 
187 
187 
188 
188 
188 
188 
189 

Date. 

Hour. 

1896 
Mar.     9 
"  9-10 
9 

'       10 
"        10 

"     10 

"  10-11 
"       10 

"     II 
"     II 
"     II 

"  I  I-I2 
"       II 
"       1  2 
"       12 
"       12 
"  12-13 
'       12 
"       13 
'       13 
'       13 
'       13 
'       M 
'       14 
'       14 
'       M 
'        M 
'       M 
'       '4 
'       M 

"      16 

"     16 

"    ie 

"      1  6 
"     16 
"      16 
"      16 
"      17 
'"      17 
'      17 
"      17 

'      1? 
1              '      17 
)            "      17 
)            "      18 

"      18 

!                "       18 

i            "     18 
)            "      18 
,            "     18 
3            "     19 
3            "     19 
•             '     '9 
'      19 
t             '     '9 
'     19 
'     !9 
j             '     19 

5                "20 

5            "     20 
I            "     20 

3.30  P.M. 
3.30  P.M.  10  3.  10  P.M. 
5.07  P.M. 
10.23  A.M. 
1-35  P.M. 
3-10      " 
3.  IO  P.M.    to  3.2O  P.M. 
5.17  P.M. 
10.23  A.M. 
I  .30  P.M. 

3  .  20     " 

3.20   P.M.    10  3.26   P.M. 
5.II    P.M. 
10.  IS  A  M. 
12.57   P  M. 
3.26       " 
3.26  P.M.   to  3.  15   P.M. 
5.13  P.M. 
10.32  A.M. 
I  .12  P  M. 
3-15      " 
5.03      " 
9.  30  A.M.  to  10.30  A.M. 
10.30  A.M. 
10.30  A.M.   to   I.OSP.M. 
I  .08  P.M. 
1.  08  P.M.   to  3.15  P.M. 
3.15  P  M. 
4.02      " 
4.52      " 
9.00  A.M.   to  10.28  A.M. 
10.28  A.M. 

10.28  A.M.  to  1.  12  r.M 

I  .  12  P.M. 
I  .  12  P.M     to  3.15  P.M. 
3.15   P.M. 
5-05      " 
9.  2O  A.M.   to   IO.27  AM 
10.27  A.M. 
IO.27  A.M.  to    I.I4  P.M 
I.  [4  P.M. 
I  .  14  P.M.   10  3.16   P.M. 
3.18  P.M. 
5-13      " 
IO.23  A  M. 
10.28  A.M.   to  I.  08  P.M 
I.oS  P.M. 
I  .08  P.M.    10  3.24  P  M. 
3.24  P.M. 
5.02      " 
g.OOA  M.  to  IO.4JA.M 
II  .08  A.M. 
12.27  P.M. 
10.45  A.M.  to  12.27  P-M 
3.02  P.M. 
12.27  P.M.  to  3.02  P.M 
5.O2  P.M. 
3.02  P.M.   to  5.02  P.M. 
g.OOA.M.    "    IO.25A.M 
10.25  A.M 
IO.25  A.M.  to  1.  08  P.M 

5  -° 
4-4 

4-5 
3.0 
4-5 
5  -° 
5-  5 
5.0 
4.0 
6.0 
4.0 
5-4 
3-5 
5-0 
5.0 
5.0 
4.8 
4.0 
21  •  5 

25.0 
24.5 
24.0 

23.6 
23.6 

23-5 
25.0 

•>4  6 

IOI    j. 

6h.  0501. 

9367 

C. 

c. 
c. 
c. 

c. 
c. 
c. 

c. 
c. 
c. 

c. 
c. 

c. 

c. 

• 

c. 
c. 

)C. 
>|C. 

c. 

> 
)C. 

99    • 
93 
99 

IOI 

103 

IOI 

97  i 
105 
97 
103 
95 

101 
IOI 
IOI 
100 

97 

87  • 

IOI 

99 
97 
95 
95 
95 
IOI 

7h.  42m. 
gh.  28m. 
2h.  oom. 
3h.  3jin. 

ii  739 
14307 
2980 
5400 

jh.  42m. 
7h.  i8m. 
loh.  O2m. 
i  ih.  52m. 

8670 
ii  080 
15  290 

1  8  060 

13)1.  43m. 
53"i- 
3h.  32111. 
6h.  01  m. 

7h.  48m. 
04111. 
2h.  44m. 
4(1.  47m. 
6h.  35111. 

20  6go 
i  303 
5  213 
8903 

ii  543 
104 
4274 
7234 
9854 

Sh.  3201. 

12  664 

58m. 

I  428 

24.5 
25.0 
25.  u 

99 

IOI 
IOI 

3h.  0501. 
3h.  5201. 
4h.  42m. 

4  54t 
57of 
6  giC 

23.  c 
24.  c 

25.  c 

24.- 

24.  c 
24.  c 
23-: 
23.? 
24-1 
24.  c 

24.1 
24- 

23.  c 
24.  c 

24. 
24. 
23.  ( 
24. 
24. 

23. 

24. 
24. 
24. 
24- 
24. 
19. 

22. 
24. 
24. 
22. 

93 
97 

IOI 
100 

97 
97 
94 
95 
:     99 
!     9? 
97 
99 
>      93 
>      97 

i    gg 

99 
)      97 
>      99 
99 
>      95 
3      97 
>      97 
97 
5      99 
>      97 
3      77 
2      go 
7    too 
>     97 
3      g2 

,  .  .  .      6h.  24111. 

9  4&f 

53m- 

i  39C 

....       2h.  56m. 
.  .  .  .      4h.  46m. 

443: 
702; 

.  .  .  .      6h.  3Sm.     967; 

.  .    ,     2h.  0401.     305. 

4h.  oSm. 
6h.  O3m. 
49m 

6134        67 
8  784        6c 
i  197        i/ 

22 

3h.  2gm 

5  19 

J.       41 

4: 

7        3f 
7        4' 

IV 

5h.  45m 
7h.  23m 

844 
1077 

09  m 
ih.  28111 

210,       26C 
2  1  2O    I  20C 

53C 

4h.  O4m 

5  840   115 
j  I  2O( 

6h.  O3m 

8  510        22 
.  .     .  .  i  I  OO( 

58 

48m 

I  220        8o< 

8oc 

COMPOSITION  OF  OHIO  RIVER    WATER   AFTER   PURIFICATION. 

TABLE  No.  4. — Continued. 
Jewell  System. 


157 


1 

a 
z 

j_ 

1895 
1901 
1902 
1907 
1908 
1913 
1914 
1919 
1920 
1922 
1923 
1931 
1936 
1937 
1941 
1942 
1947 
1948 
1954 
1955 
J959 
1962 
1964 
1969 
'973 
1983 
1989 
1993 
1998 
200  1 
2005 
2008 

2OI2 
2OI4 
2OI5 
2016 
20I7 
2018 
2Olg 
2021 
2023 
2024 
2025 
2026 
2O27 
202S 
2O29 
2033 
2035 
2040 
2043 
2047 
2050 
2054 
2057 
2065 
2076 
2083 
2099 
2103 
2106 
2110 
2121 

Collected. 

Number 
Run. 

Rate  of 
Filtration. 

b 

T3 

a 
1 

Period  of 
Service  Since 
Last 
Washing. 
Hours  and 
Minutes. 

^  si 

^» 
I.JU 

tL, 

.a 

£t 
3 
U 

s.5 

is 
M^ 

m 

Remarks. 

I 

Is 

L> 

Is- 
]{I 

Date. 

Hour. 

1896 
Mar.  20 

"         20 
"         20 
"         20 
20 
"         2 
"         2 
"         2 
"         2 
"         2 
"        2 
"        2 
"       23 
23 
'        23 
23 

1     23 
'    23 
23 
1    23 
24 
24 

1       24 

24 
24 
24-25 

25 

1     25 

1       25 

'       25 

1     25 
25 

"       25 

"     26 

"        26 

"     26 
'•     26 
"     26 
"     26 
25-26 
"    26 
"     26 
"     26 
"     26 
••     26 
"     26 
"     26 
"     26 
"     26 
"     26 
"     26 

;;  26 

26 
"     26 
"     26-27 

;;  27 

27 

1   27 

,   27 

27 

::  2? 
27 

"  27-28 

I.OS   P.M. 
1.  08  P.M.    to  3.33  P.M. 

3  33  i'-M. 
4-53     " 
3-33    P.M.  to     5.30   P.M. 
g.OO  A.M.    "    10.45  A.M. 
10.45  A.M. 
12.58    P.M. 
IO.45  A.M.  to  12.58    P.M. 

12.58  P.M.  "     3.20     " 

3.20  P.M. 
3-20    P.M.    to      5.00  P.M. 
g.OO  A.M.     "     10.25  A.M. 
10.25  A.M. 
10.25  A.M.    to   12  M. 
12.00  M. 
12.  OO  M.   to  3.OO  P.M. 
3.OO  P.M. 
5.16       " 
3.00   P.M.   to      5.30    P.M. 
g.OO  A.M.     "     II.  30  A.M. 
11.30      "        "      2.30   P.M. 
2.30   P.M.    "      4.42      " 
442       "        "      8.30      " 
8.30      "        "    II   30      " 
11.30      "        "      2.  30  A.M. 
2.30  A.M.   to     5.30  A.M. 
5.30      "        "      8.30      " 
8.30      "        "    11.30      " 
11.30      "       "      2.30  P.M. 
2.30   P.M.    "       5.30      " 
5.30      "       "      8.30      " 
8.30      "        "    11.30      " 
I  00  A.M. 
1.  08      " 
1.18     " 
1-33     " 
1.48     " 
2.18     " 
11.30  P.M.  to  2.30  A.M. 
2.48  A.M. 
3.48       " 
4.14       " 
4.48       " 

5-15     ' 
5-3°     " 
2.30  A.M.  to  5.30  A.M. 
5-49  A.M. 
5.3O  A.M.    to     8.30  A.M. 
8.30      "        "    11.30      " 
II.3O      "        "      2.30   P.M. 
2.30   P.M.    "      5.30      " 
5.30      "       "      S-30      " 
8.30      "        ''    11.30      " 
11.30      "       "      2.30  A.M. 
2.30  A.M.    "      5.30      " 
5-30      "        "      8.30      " 
8.30      "        "    11.30      " 
11.30      "       "      2.30   P.M. 
2.30   P.M.    "       5.30      " 
5.30      "        "      8.30      " 
8.30      "        "    11.30      " 
II.3O      "       "      2.3O  A.M. 

66 
66-67 

67 
67 
67 
67-68 
68 
68 
68 
68-69 
69 
69 
70 
70 
70 
70 
70-71 
71 
72 
71-72 
72 
72-73 
73 
73-74 
74 
74-75 
75 
75-76 
76 
76-77 
77 
77-78 
78 
79 
79 
79 
79 
79 
79 
78-79 

79 
79 
79 
79 
79 
79 
79 
79 
79-80 
80-8  1 
81-82 
82-83 
83 
84 
84 
84-85 
85 
86 
86 
87 
87-88 
88 
88-89 

24.0 
23.1 
23.0 
23-5 

24-3 
23.2 
24.0 

21.0 
22.6 
22.8 
24.0 
22.0 

23  6 
21.0 
21.2 
25.0 
23.3 
24.0 
24.5 
24.9 
25.5 
23.7 
21.4 
25-4 
22.6 
23.4 
23.2 
23.8 
24.9 
25.8 
24.3 
25.6 
24.2 
25.0 
25.0 
25.0 
25.0 
25.0 
25.0 
22.8 
25.0 
24.5 
24  5 
24.5 
25-5 
24-5 
23.6 
23.0 
23.0 
26.5 
23.3 
24.1 

2I.I 

24.7 

20.1 
23.2 
23.6 
24.0 
23.8 
21-5 

24.2 

23-5 

23-5 

97 
93 
93 
95 
98 
94 
97 
85 
9i 
92 
97 
89 
95 
85 
86 

IOI 

94 
97 
99 

IOI 

103 
95 

86 

IO2 
91 

94 
94 
96 

IOI 

104 
98 
103 

98 

10 
10 

IO 
10 
10 
10 

92 

IOI 

99 
99 
99 
103 
99 
95 
93 
93 
107 
94 
97 
89 

IOO 

89 
94 
96 
97 
96 
87 
98 
95 
95 

24111. 

593 

600 

I  OOO 
I  000 
I  000 
I  2OO 
495 
415 
465 
860 
895 
I  905 
785 
440 
405 
700 
I  250 
800 
475 
i  245 
I  230 
179 
So 
270 
132 
74 
306 
i  030 
495 
48 
158 
405 
178 
107 
156 
113 
171 
229 
420 
345 
215 
600 
435 
460 
415 
232 

221 
482 
124 
171 

355 
700 
520 
805 
330 
477 
485 
575 
415 
128 
i  650 
150 
H7 
540 

C. 

C. 
C. 

[layer  at  11.25  A.M. 
Agitated  surface  of  sand 
C. 
C.   Agitated   surface    of 
sand  layer  at  3.05  P.M. 
C. 
C. 

C.    Agitated    surface   of 
sand  layer  at  10.29  A.M. 
C. 
Agitated  surface  of  sand 
layer  at  3.30  P.M. 
C.       [layer  at  10.36  A.M. 
Agitated  surface  of  sand 
[layer  at  3.54  P.M. 
Agitated  surface  of  sand 
[layer  at  9.30  P.M. 
Agitated  surface  of  sand 
[layer  at  3.41  A.M. 
Agitated  surface  of  sand 
[layer  at  11.05  A.M. 
Agitated  surface  of  sand 
[layer  at  3.51  P.M. 
Agitated  surface  of  sand 
[layer  at  10.36  P.M. 
Agitated  surface  of  sand 
This  series  of  results  on 
run   No.   79  was    used 
in  obtaining  the   aver 
age    bacteria    for   this 
run,    but    not    for   the 
day. 

Agitated  surface  of  sand 
layer  at  4.07  A.M. 

[layer  at  7.47  P.M. 
Agitated  surface  of  sand 
[at  1  1.  54  P.M.  &  2.  1  1  A.M. 
Agitated  surface  of  S.L. 
[layer  at  6.15  A.M. 
Agitated  surface  of  sand 
[layer  at  11.33  A'M- 
Agitated  surface  of  sand 
[layer  at  5.55  P.M. 
Agitated  surface  of  sand 
Agitated  surface  of  sand 
layer  at  10.08  P.M. 

05  m. 
ih.  25m. 

"3 

2053 

45m. 
2h.  55m. 

I  085 
4095 

.  .  .  .       ih.  4im. 

2371 

ih.  47m. 

2  5'4 

3h.  2om. 

5874 

ih.  4om. 
46m. 

2  421 
I  071 

I2m. 
2om. 
3om. 
45m. 
ih.  oom. 
ih.  3om. 

419 

579 
829 
I  179 
i  579 
2339 

2h.  oom. 
3h.  oom. 
3h.  23m. 
3h.  57m. 
4h.  25m. 
4h.  39m. 

3049 
4529 
5049 

5789 
6429 
6789 

4h.  58m, 

7159 

WATER  PURIFICATION  AT  LOUISVILLE. 

TABLE  No.  4. — Continued. 
Jewell  System. 


.0 
8 

2; 

Collected. 

Number 
Run. 

Fill 

1  a! 

^   3 

11 

CJ 

o  a 

6   5   D 

r-  <    3 
5    ul 

fe 

— 
j 

c 
Period  of        "C  % 

Washing.       ^Jt 
Hours  and       ^  o 
Minutes.     1    £  g| 
—  i-iu 
!b 

!S 

u  u. 

«  ^ 

e 

Remarks. 

Date. 

Hour. 

2127 
2131 
2136 
2139 
2143 
214(3 
2148 
2149 
2150 
2151 
2152 
2155 
2158 
2161 
2165 
2169 
2173 
2182 
2185 
2189 
2192 
2196 
2199 
2203 
2206 

22IO 
2216 
2220 
2224 
2229 
2234 
2237 
2242 
2247 
225(1 
2255 
2262 
2257 
2271 
2276 
2281 
2286 

2289 
2294 
2299 

2302 

2306 
2307 
2308 

2310 
2322 
2323 
2324 
2325 
2326 
2327 
2328 
2329 
2331 
2334 
2338 
2340 
2341 

1896 
Mar.  28 

"      28 
"      28 
"      28 
"      28 
"      28 
"      28 
"      28 
"      28 
"      28 
"      28 
"      28 
"   28-29 
"      29 
"      29 
'      29 
'      29 
'      29 
"     29 
"      29 
"    29-30 
"      3° 
"     3° 
"     30 

•'     3° 
"     3° 
"     31 
"     3i 
"     31 
April    i 
"        i 

"           2 
"          2 
2 

"       3 
3 
4 
4 
4 
6 
6 
6 
7 
7 

::  ! 

::  5 

8 
8 

(<                g 

8 
8 
"       8 
8 
8 
8 
8 
9 
9 
9 
"       9 

2.30  A.M.   to      5.30  A.M. 
5.30      "        "      8.30     " 
8.30  A.M.     "   11.30  " 
II.3<>       "         "      2.30    I'.M. 
2.30   I'.M.      "      5.30      " 
5.30       "         "      8.30      " 
IO.25    I'-M. 
10.35        " 
10.45        ' 
10-55        ' 
II.O5        " 
8.30    I'.M.    to   II.3O   I'.M. 
11.30       "         "      2  30  A.M. 

89 
89-90 
90 
90-91 

91 
91-92 
92 
92 
92 
92 
92 
92 
92 

23.8 
24.8 

23-9 
22.9 

24-5 
24.2 
25.0 
25.0 
24-5 
24-5 
24-5 
23-4 
22.5 

96 

100 

97 
93 
99 
98 

IOT 
10  I 

99 
99 
99 
95 
91 
08 

407 
321 
238 
62 
119 
174 
261 
1  86 
3'3 

221 
2-13 

193 
119 

234 
177 
294 

580 

595 
240 
4<>5 
125 
256 
476 
58l 
785 
672 
650 
390 
I  495 
845 
545 
525 
240 
224 
205 
92 
310 
60 
62 
90 
30 
36 
27 
30 
44 
118 
53 
82 
88 
76 
65 
20  1 
1  86 
125 
104 
194 
185 
75 
63 
72 
157 
182 
152 

Agitated  surface  of  sand 
layer  at  3.41  A.M. 
Agitated  surface  of  sand 
layer  at  9.26  A.M. 
Agitated  surface  of  sand 
layer  at  4.11  I'.M. 
C.  Agitated  surf,  of  sand 
C.      layer  at  10.  n  P.M. 
C. 
C. 
C. 

Agitated  surface  of  sand 
layer  at  6.17  A.M. 
Agitated  surface  of  sand 
layer  at  2.14  I'.M. 

Agitated  surface  of  sand 
layer  at  9.31  P.M. 

Agitated  surface  of  sand 
layer  at  5.58  A.M. 
Agitated  surface  of  sand 
layer  at  2.01  I'.M. 
Agitated  surface  of  sand 
layer  at  10.01  A.M. 
Agitated  surface  of  sand 
layer  at  3.05  P.M. 
[layer  at  2.39  P.M. 
Agitated  surface  of  sand 
[layer  at  11.25  P.M. 
Agitated  surface  of  sand 
[layer  at  11.54  A.M. 
Agitated  surface  of  sand 
Agitated  surface  of  sand 
layer  at  4.27  P.M. 
Agitated  surface  of  sand 
layer  at  1.09  P.M. 
Agitated  surface  of  sand 
layer  at  9.00  A.M. 
Agitated  surface  of  sand 
layer  at  2.09  I'.M. 
Agitated  surface  of  sand 
layer  at  12.07  v.M. 
Agitated  surface  of  sand 
layer  at  11.42  A.M. 

C. 
C. 

C. 
C.  Agitated  surf,  of  sand 
layer  at  10.17  A.M. 

2h.  42tn.    3  826 
2h.  52111.    4  126 
3h.  02m.    437<> 
3h.  13111.   455f' 
3h.  22m.   4  804 

5.30       "         "      8.30      " 
8.30       "         "11.30      " 
11.30       "         "      2.30    I'.M. 
2.30    I'.M.      "      5.30      " 
5.30       "         "      8.30      " 
8.30       '           "    11.30      " 
11.30       "         "      2.30A.M. 
2.3O  A.M.      "      5.30      " 
5.30       "         "      8.30      " 
8.30       "          "    11.30      " 
11.30       "         "      2.30    I'.M. 
2.3O  I'.M.      "      5.30      " 
9.15  A.M.      "   11.30  A.M. 
11.30       "         "      2.30      " 
2.30    P.M.      "      5.30   I'.M. 
9.  15  A.M.      "11.30  A.M. 
II.3O       "         "      2.30   I'.M. 

2.30  P.M.    "     5  30    " 

9.30  A.M.      "    I  1.30  A.M. 
II.3O       "         "      2.30    I'.M. 
2.30    I'.M.      "      5.30      " 
9.20  A.M.      "    11.30  A.M. 
2.30   I'.M.      "      5.30  P.M. 
9.30  A.M.      "    11.30  A.M. 

11.30     "      "    2.30  P.M. 

2.3O   I'.M.     "      5.30      " 
9.2O  A.M.      "    II.3O  A.M. 
11.30       "         "      2.30    I'.M. 
2.30   I'.M.      "      5.30      " 
9.25  A.M.      "    11.30  A.M. 
II.3O       "         "      2.30    I'.M. 
2.30       "         "      5.30      " 
I  I  .  OO  A.M. 
II.  TO       " 
II.  2O       " 
9.2O  A.M.    to   II.3O  A.M. 
11.30       "         "      2.30  I'.M. 
3.32    I'.M. 
3-35       " 
3.38       " 
3-41       ' 

3-44      ' 
3-59     " 
4.14     ' 

2.3O   P.M.    to       5.30    I'.M. 
9  2O  A.M.     "    11.30  A.M. 
11.57  A.M. 
12.32    P.M. 
I.  O2       " 

93 
93^94 
94 
94 
94-95 
95 
95-96 
96 
96 
90-97 
97 
98 
98 
99-100 

IOO-IOI 

102-103 
104 
104 
105 

105-106 
1  06 
106-107 
108 
108-109 

101) 

109-1  10 

I  IO 
IIO-I  1  1 

1  1  1 

112 
I  12 
II2-II3 
1'3 
I'3 

"3 

113 
113 
114 
114 
114 
114 
114 
114 
114 
113-114 
114 

'14 
114 
114 

24-1 

23-9 
23-9 

25-1 

23-5 
27-5 
22.7 
24-6 
23-8 
23-7 
24-4 

25-1 
24-2 

23.3 

24-0 

23-7 

23-2 
23-1 
24-0 
24-0 

24  3 

24.7 

24-3 
23-7 
25  8 

23-2 
23-9 
25-2 
22-9 

24-8 
24-4 
24-3 
25-5 
24-5 
24-0 
24-3 
24-7 

22.  O 
24-0 

:?.o 
25.0 
25.0 
25-0 
25.0 
23-4 
24.0 
24.0 
24.0 
24.0 

98 
97 
97 

IOI 

95 
ii  i 
92 

99 
96 

95 
99 

IOI 

97 
94 
97 
95 
93 
93 
97 
97 
98 

IOO 

98 
96 
104 
94 
97 

IOI 

93 

IOO 

98 

97 
103 

99 
97 

98 

IOO 

89 
97 

IOI 
IOI 
IOI 
IOI 
IOI 

95 
97 
97 
97 
97 

.. 

i 





3h.  26m.    5  014 
3h.  36m.   5  244 
3h.  46m.    5  494 

03111.         6  1 
(  6m.       131 
09111.       211 
12111.       291 
15111.:     361 
30111.       711 

45111.     I  IOI 

4h.  5&m.    7  121 
5h.  3im.   7961 
6h.  Dim.  8  621 

COMPOSITION  OF  OHIO   RIVER    U'ATER  AFTER   PURIFICATION. 


'59 


TABLE   No.  4. — Continued. 

Jewell    System. 


I1 

. 

S 

Collected. 

Filtration. 

«> 

c 

.i 

• 

~^  5T^— 

Period  of        1'  i 

"§ 

1 

\-  .     i 

e. 

5  & 

TJ 

Service  Since     fi  -;:,_; 

U  ^ 

g 

""of"" 

„ 

Last            5  H  S 

a  " 

Remarks. 

'       Run. 

Washing.       Sjgfc. 

y. 

Date. 

Hour. 

ul 

its    "s 

Hours  and      ~af  u 

-  ~ 

•c 

•Spr 

ii  a?'     " 

~23 

"u 

X 

U 

7.         ',     2 

fb 

03 

1896 

234J 

April    9 

1  1  30  A  M     to     2  30   P  M       I  14—1  15  °3    4 

nc 

102      C. 

2346 

9 

2.30P.M.    "     5.00     "            115      23.6      95     .... 

n>6    C.  Agitated  surf,  of  sand 

2349 

'       o 

0.15  A.M.                        115      '24.0      97     .... 

3h.  3im. 

4983 

62 

layer  at  4.32  P.M. 

2351 

0 

0.45     '                          U5      24.0      97     

4h.  oim. 

5  683      33 

2353!       '    ° 

1.15      '                          "5      24.0      97     

4h.  3im.     6  313 

28 

2356            '       o 
2368           "       o 

1.45      '                          US      25.0    ioi   ;  

TT    TO          V      t(l       ?    1O    I'    \f                IIC          m      T          m 

5h.  oim.     6973      39 

C. 

2374                 "          O                  2   1O         \f        "       C    1O       "                  I  1  ft         "II          (17 

C. 

2380          " 

9  20  A  M     "  1  1  30  A  M          116      24  5      99 

•  -j 
9c 

-  J^>^> 

2382. 

12.05  P.M.                        116       24.0      97     .... 

6h.  oim.     8  765      42 

layer  at  9.00  A.M. 

2384 

12.35      '                          116      1.4.0 

97     .... 

6h.  3im. 

9454      23 

2386 

1.05     '                       1  16     23.5 

95 

7h.  oim. 

10  118      31 

2388] 

1.35      " 

116      23.0 

95     .... 

7h.  3im. 

10  905      30 

Shut      inlet      1.34      P.M., 

2389 

2.01        ' 

117      24.0 

97     .... 

O3m. 

43       78 

outlet  1.45  P.M. 

2390 

2.04       " 

117      25.0 

IOI 

06  m. 

123      So 

2391 

2.07    " 

"7      25.0 

lot 

09111. 

193 

57 

2392 

1                                             2.10       " 

117      24.0 

97 

1  2  in  . 

263 

32 

2393 

2.13       " 

117      24.0 

97 

15111. 

343 

38 

2394 

'                                             2.28       " 

117      24.0 

97 

3<>m. 

7°3 

31 

2395 

2.43       " 

117      24.0 

97 

45m. 

i  093 

37 

2397 

"                               TT    -3O    P   M      to       2    1O    l>   M 

1  1  6—  117  24.0 

O7 

J7 

C. 

2399 

3.13    P.M. 

117      24.0 

V/ 

97 

ih.  ism. 

2  793 

4  / 

27 

2405 

3.58       " 

117       24.0 

97 

2h.  oom. 

2903 

24 

2408 

' 

4.28       " 

"7 

24.0 

97 

2h.  3om. 

3  633 

43 

2410          "                             4.58     " 
2412            ''                  ;   2.30  P.M.  to     5.30  P.M. 

117      24.0 

T  T  7         o  1  .  r, 

97 
97 

3h.  oom. 

4363 

38 
18 

C. 

2415                "          3                9.  2O  A.M.     "    II.  30  A.  M.I          118        °  <    ^ 

m 

32 

c. 

2417!           "       3           11.30     "       "     2.30  P.M.!        118 

-t  •  *-»      j  i 

2.1    T       Q8 

j~ 

S3 

2419            "       3                         4-55  I'.M.                       118 

^4  -  J       v° 

23.0       93 

6h.  4im.     9640 

81 

layer  at  11.53  A.M. 

2422               "         4                            11.30  A.M. 

IIS 

22.  O 

89 

8h.  03m.    II  617 

13 

2424               "         4                               2.56  P.M. 

119 

22.0        8() 

2h.  24m.  !    3  401 

41 

[layer  at  4.51  P.M. 

2425!                "           4                                     5.00       "                                     IK)         22.0         89 

4h.  26111. 

6i73 

29 

Agitated  surface  of  sand 

2428            "        5                       10.45  A.M.                      119      25.0    ioi 

6h.  41  m.     7  630 

20 

[layer  at  i  26  P.M. 

2429            "        5                         2.43  P.M.                       119      25.  o:    ioi 

loh.  3801.  !  13  409 

20 

Agitated  surface  of  sand 

243i:           "       5                         4-54     "                         "9      25.  0;    ioi 

I2h.  4/111.    id  i6n 

20 

Ag.  surf.  S.  L.  4.53  P.M. 

2434'            '       6                       10.40  A.M.                      119      23.0      93 

I5h.  osm. 

19960 

15 

Shut  in!.  10.3,,,  outl.  10.4^  A.M. 

2435             '       6                        3-05  I'.M.                        20      25.0    ioi 

4h.  <x)in. 

5884 

14 

Agitated  surface  of  sand 

2437            "       6                         5.00     "                           20 

25.0    ioi 

5h.  56m. 

8714        5 

layer  at  2.36  P.M. 

2440                "          7                               10.40  A.M.                                 2o 

24.5 

99 

8h.  0501. 

2441                 "          7                                 2.41    P.M.                                 21 

24-5 

99 

ih.  oom. 

I    (121 

44 

2443                "          7                                 4-4"       "                                     21 

24.5 

99 

3h.  osm. 

4501 

44 

2446,                 '          8                               10.35  A.M.                                 21 

24.5 

99 

5h.  3801. 

7991 

152 

Agitated  surface  of  sand 

2447            "       3                         2.40  P.M.                        21 

25-0 

IOI 

9h.  33m. 

I407I 

96 

layer  at  10.33  A.M. 

2449             '8                         5.15     '                            21 

25.0 

IOI 

I2h.  o6m. 

I794I 

53 

Agitated  surface  of  sand 

2453.               "       2O                               IO.3O  A.M.                                 22 

25.0 

101        .... 

ih.  07m. 

1    676 

4 

layer  at  3.58  P.M. 

2454                "       20                               11.55       "                                     22 

25.0 

IOI      .... 

2h.  3201. 

3  73''        8 

2459,               "       20                                 2.55    P.M.                                 22 

25.0 

101 

5h.  iSm. 

7  696!       6 

Agitated  surface  of  sand 

2460                 '20                                 5.  If)       "                                     22 

25.0 

101        .... 

7h.  39m. 

ii  186'       6 

layer  at  2.04  P.M. 

2464 

"      21 

9  34  A.M. 

22 

25.0 

IOI      .... 

8h.  27m. 

12396!       6 

2466 

"      21 

10.25      ' 

22 

25.0 

IOI      .... 

9h.  18111. 

1  3  filili          19 

2469 

"       21 

12.41    P.M. 

23 

25.0 

IOI      .... 

1  1  in. 

247 

24 

2473 

"       21 

1.50      " 

23 

25.0 

IOI       .... 

ih.  2om. 

1967 

670 

2476 

"       21                                  2.59       " 

23 

25.0 

IOI      .... 

2h.  29m. 

3667 

17 

2477 

"       21                                  5.11 

23 

24.0 

97    

4h.  40111. 

6857 

21 

Agitated  surface  of  sand 

2480 

"      22                              9.54  A.M. 

23 

25.0 

IOI 

MI.  53m. 

8657 

24 

layer  at  4.39  P.M. 

2482 

"      22                            10.48       " 

23 

25.0 

101 

6h.  47m.     9  987 

19 

2485 

"      22                            12.39  I'.M. 

23 

25.0 

IOI 

8h.  38m.    12  727 

II 

2487 

"      22                               1.24      " 

23 

25.0 

IOI 

9(1.  2301.!  13  807 

8 

249O 

"      22                               3.00      " 

23 

24.0 

97 

loh.  59m.    16  187 

17 

Agitated  surface  of  sand 

2493 

"       23                                 9.42  A.M. 

23 

24.0 

97 

13(1.  oom.   20857 

21 

layer  at  3.58  P.M. 

2494 

"       23 

IO.23      " 

23 

24.0 

97 

14!).  50111. 

21  887 

20 

Agitated  surface  of  sand 

2498 

"       23 

12.53   I'-1'. 

24 

23.0 

IOI 

28m.        675      32 

layer'at  10.46  A.M. 

2500 

"       23                                 2.03       " 

24 

24.0 

97 

ih.  38m.  I    2  405'     14 

i6o 


WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE    No.  4. — Continued. 
Jewell  System. 


Collected. 

Ra 

Fill 

teof 

b 

Period  of 

c 
'&  to 

.0 
3 

z 
in 

Date. 

HOU, 

Number 
Run. 

Q. 
>f-  3 

15^ 

3  *^ 
U 

Jo. 

5s  3 

0  ^X 

|JU 

I 
J 

Last 
Washing. 
Hours  and 
Minutes. 

91 

rS>3u 

g 

0$ 

CO 

Remarks. 

2503 
2505 
2509 
2511 
2514 
2517 
2519 
2525 
2527 

1896 
Apr.  23 
"     23 
"     24 
'     24 
"     24 
'     24 
"     24 
"     25 
"     25 

3.06  P.M. 
4.50      " 
9.37  A.M. 
II    46      " 

i  .  14  P.M. 
[2.49    " 
4-44     " 
12.45    " 

2.57     " 

124 

124 
124 
124 
124 
124 
124 
125 
125 

25.0 
24.0 
25.0 
25.0 
25.0 
25.O 
25.0 
25.0 
25.0 

101 

97 

IOI 
101 
IOI 
IOI 
IOI 

lor 

IOI 

2h.  4im. 
4h.  25m. 
5h.  42m. 
7h.  49111. 
gh.  I7m. 
loh.  42m. 
I2h.  47m. 
ih.  O7m. 
3h.  igm. 

3985 
6515 

8  865 
11585 
'3  795 
16235 
'9  '55 
i  773 
5047 

24 
28 

67 

41 
32 

37 
52 
56 
4' 

Agitated  surface  of  sand 
layer  at  10.06  A.M. 

[layer  at  7.46  P.M. 

"  27-28 

g.OO      "       "    3.OOA.M. 

"      28 

25  6 

"     28 

"     28 

2551 

"  28-29 

9.OO      "        "    3.OO  A.M. 

128 

24.9 

IOO 

Agitated  surface  of  sand 

"     29 

3.OOA.M.    "    g.OJ      " 

128 

25.6 

2561 

"     29 

9  .  oo    "      "   3  .  oo  P.  M  . 

128-129 

25.3 

IO2 

[at  4.03  P.M.  and  8.34  P.M. 

2565 
2566 
2567 
2568 
2569 
257° 
2571 
2372 
2573 
2574 
2575 
2576 

2577 
2579 
2580 
2581 
2582 
25S3a 
2583b 
2584 
2585 
2586 
2589 

0 

10.39  P'M- 

11.05    " 
11.07    " 
1  1  .  09    " 
II  .  1  1    " 
11.13     " 

11.15    " 
11.17  " 

II.  19    " 

I  I  .  21       " 
II  .23      " 
11.25      " 
11.27      " 
11.29      " 
11.31       " 
11.33      " 
11.38      " 
11.48      " 
I2.O3  A-M- 
1.03      " 
2.O3      " 
g.OO  I'.M.    to   3.OO  A.M. 

129 
129 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 
130 

24.6 

22.0 
28.0 
26.0 
J7.0 
26.0 
26.O 
26.0 
26.0 
26.0 
26.0 
26.5 
26.5 
26.5 
27.0 
27.0 
27.0 
27-5 
27.0 
26.5 
26.O 
26.0 
25.6 

99 
89 
114 
105 
log 
105 
105 
105 
105 
'05 
105 
107 
107 
107 
109 
log 
109 
III 
log 
107 
105 
105 

I2h.  3001. 
O2m. 
O4tn. 
06m. 
o8m. 
lorn. 
I2tn. 
14111. 
1  6m. 
i8m. 

2O111. 
22111. 

24m. 
26m. 
28m. 
30  in. 
35"i. 
45m. 
ih.  oom. 
2h.  oom. 
3h.  oom. 

18788 
56 
106 
156 
216 

266 

316 
366 
426 
476 

526 

576 
636 

686 
736 
7g6 
g26 
I  1  86 
i  5g6 
3  116 
4676 

102 
139 

86 
86 
70 
49 
58 
38 
36 
39 
24 
44 
33 
"3 
26 

30 
38 
29 
26 
26 
24 
74 

The  series  of   results  on 
run   No.  130  was  used 
in  obtaining   the  aver 
age  bacteria  for  the  run 
but  not  for  this  day. 

« 

2590 
2591 
2592 
2593 
2594 
2595 

"    30 
"   30 

"     3° 
"     30 
"     30 
"     30 

3.03  A.M. 
4.03      " 
5-03      " 
6.03      " 
7-03      " 
8.03      " 

130 

130 
130 
130 
130 
130 

26.0 
26.0 
26.0 

26.0 
26.0 
26.0 
26  o 

105 
105 
105 
105 
i°5 
105 

4h.  oom. 
5h.  oom. 
5h.  58111. 
6h.  sSm. 
7h.  58111. 
Sh.  58111. 

6  206 
7  786 
g  226 
10  816 
12  346 
13956 

52 
23 
27 
53 
8g 
34 

Agitated  surface  of  sand 
layer  at  4.44  A.M. 

26OO 

"     30 

12.57  P.M. 

130 

22.5 

91 

I3h.  5201. 

21  406 

23 

[layer  at  8.46  P.M. 

2608 

"     30 

25.6 

46 

Agitated  surface  of  sand 

264O 

65 

Agitated   surf,  of  sand   layer 

26  6 

67 

78 

Ag  surf  of  s  I.  at  1.14  A.M. 

266O 

"          2 

46 

[layer  at  3  07  P.M. 

2666 

78 

28   i 

2674 
2675 
2676 
2677 
2678 

4 
4 
4 
4 
4  ' 

7.30  P.M. 
17-32      " 
7-34     " 
'7.36     " 
t7.3S     " 

'34 
134 
"34 
134 
134 

25.0 
25.0 
25.0 
25.0 
25.0 

10 

10 

10 
10 
10 

O2m. 
O(m. 
o6m. 
o8m. 
'iom. 

53 
113 
183 
223 
263 

116 
M9 
132 
61 
65 

From  May  2-9,  inclusive,  the 
results  of  both  single  sam 
ples  and  ihose  collected  by 
the  sampler  were   used   to 
obtain    the   bacterial    aver 
ages  for  days  and  for  runs. 

COMPOSITION  OF  OHIO  RIVER    WATER   AFTER   PURIFICATION. 


161 


TABLE  No.  4. —  Continued. 
Jewell    System. 


Collected. 

R 

Fil 

ate  of 

£ 

1 

5 

• 

u 

01 

i 

s 
z 

Date. 

Hour. 

Number 
of 

& 

£~ 

u  c 

Ss 

U 

=  $• 

C  o  = 

§*I 

=  0.3 

•o 

a: 
I 

Last 

Washing 
Hours  and 
Minutes. 

fl| 

^JU 
ta 

v  -. 

ag 

re  ^ 
X 

Remarks. 

267? 

26Sc 
2681 
2682 
2683 
268.1 
268? 
2686 
2687 
2688 
2689 
2690 
2691 

1896 
May  4 
'      4 
'      4 
'       4 
'      4 
'      4 
'       4 
'      4 
'      4 
'       4 
'       4 
4 
'       4 
'      4 

7.40  P.M. 

7.42      " 
7-44      " 
7.46     " 
7.48     " 
750     " 
7.52      ' 
7-54     " 
7-56      " 
7.58      " 
8.03      " 
8.13     " 
8.28     " 

3.15  P.M.   to  g.OO  P  M. 

134 
134 
'34 
'34 
'34 
'34 
"34 
134 
134 
134 
134 
134 
'34 
133-134 

26.  c 
26.  c 
26.  c 
26.  c 
26.  c 

27.0 

27.  c 
27.0 
26.= 

27.  c 

27.0 
27.0 
27.0 

105 
105 
i°5 
105 
105 
log 
log 
109 
107 
109 
109 
109 
109 

I2m 
14  m 
i6m 
1  8m 
2om 

22111 
24111 
2III11 

28m. 
3om. 
35m. 
45m. 
ih.  oom. 

3". 

3f>3 
42? 
473 
S-'. 
583 
<>33 
68- 
743 
793 
923 
I  193 
'593 

33 
43 
44 
32 
29 

33 

28 
30 
42 
42 
26 
39 
29 
46 

2695 
2696 
2697 
2698 
2699 
2700 

"      4 
4 
'       4 
"      5 
"      5 

'"'      3-5 

9.28  P.M. 
1028      " 
11.28       " 
12.28  A.M. 
1.28      " 
2.28      " 

'34 
134 
134 
134 
134 
134 

27.0 
27.0 
27.0 
27.0 
27.0 
27.0 

26    5 

log 
log 
log 
log 
log 
log 

2h.  oom. 
3h.  oom. 
4)1.  oom. 
5h.  oom. 
6h.  oom. 
7h.  oom. 

3203 
4823 

6453 
8053 
9663 
II  233 

37 
33 
4') 
47 
38 
go 

2704 
2703 
2706 
2707 
2708 
2709 

::  \ 

"       5 
'      5 
'       5 
'       5 
"       5 

3.28  A.M. 
4.28      " 
5.28      " 
6.28      " 
7.OO      " 
8.00     " 

134 

134 
134 
'34 
134 
134 

27.0 
27-0 
26.5 
26.5 
26.5 
27.0 

26  o 

log 
109 

107 
107 
107 
109 

8h.  oom. 
gh.  oom. 
gh.  58m. 
loh.  58m. 
nh.  58m. 
I2h.  5801. 

I28g3 
14473 
15923 
I7&53 
19163 
20773 

96 

86 
69 
28 
29 
29 
37 

Agitated    surface   of  sand 
layer  at  5.12  A.M. 

27:4 
2715 
2716 
2717 
2719 
2723 

"      5 
'      5 
'      5 
1       5 
5 
"       5 

g.2S  A.M. 
10.28       " 
11.28       " 
12.28  P.M. 
1.28       " 
g.OO  A.M.  to  3.OO  P.M. 

134 

134 
134 
134 
134 
134-135 

6.5 
26.5 
6.0 
6.5 
4-5 
6   i 

107 
107 
I°5 
107 
99 

I3h.  s8m. 
I4h.  58m. 
I5h.  5601. 
i6h.  56m. 
I7h.  54m. 

22  483 
24  143 
25633 
27  '53 
28543 

24 

58 
37 
56 
46 
40 

Agitated    surface    of  sand 
layer  at  11.19  A.M. 
Agitated    surface   of  sand 
layer  at  1.07  P.M. 

"        S 

2731 

"       5-6 

g.OO       "       "    3.00  A  M. 

3  8 

96 

56 

layer  at  4.11  P.\  . 

"      d 

5   8 

2736 

"       6 
"       6 

9.35  A.M. 

136 

136 

6.5 
6  4 

107 

ih.  4om. 

2763 

25 

layer  at  6.35  A.H  . 
Agitated   surface    >f  sand 

274.) 

6 

136 

6  4 

2746 
2749 

"       6 
"       6 

3  oo  P.M. 

3-OO  P.M.   IO  g.OO  P.M. 

136 

136 

7-0 

109 

7'n.  03111. 

II  213 

16 

"       6-7 

136   137 

85 

2753 
2759 

"      7 
"      7 

3.00  A.M. 
3  OO  A.M.  to  9  OO  A.M. 

137 
137 

-•:•" 
-   ', 

IO<) 

igm. 

5'9 

So 

layer  at   10.21   P.M.  and 

I.C8  A.M. 

2760 

2765 

"      7 

g.OO  A.M. 
g.OO  A.M.    10  3.00  ['.M. 

137 

27.0 

26  8 

109 

6h.  igm. 

10  iSg 

32 

38 

[layer  at  12.34  P.M. 
Agitated    surface   of    sand 

3.00  P.M.  "  9  (xj     " 

46 

277-1 

"       7-8 

g.OO  I'.M. 

138 
138 

26.5 

107 

o8m. 

ig2 

57 

layer    at   6.o3   and   8.25 

2780 
2705 

"      8 
"      8 

3.00  A.M. 
3.OO  A.M.  to  9  OO  A.M. 

138 
138 

-•:." 

log 

6h.  o8m. 

9852 

26 

32 

Agitated    surface   of  sand 

2786 
2792 

"      8 
"       8 

9.OO  A.M. 
9.OO  A.M.   tO  3.OO  P.M. 

138 
138 

27.0 

,-  , 

log 

nh.  4101. 

18732 

8 
18 

layer  at  S.  19  A.M. 

2793 

2-<r 

"      8 
"       8 

3.00  P.M. 

3.00  P.M.  to  9.00  P.M. 

138 

i  (8   i  i(i 

25.0 

1OI 

I7h.  41  m. 

26  732 

19 

Agitated    surface    of  sand 
layer  at  3.04  P.M. 

2803 

"      £-g 

2804 
2808 

"     f9 

3.00  A.M. 

139 

27.0 

log 

gh.  5601. 

15907 

12 

layer  at  1.45  A.M. 

2813 
2818 
2825 
2830 

9 
'      9 
"     1  1 
"     II 

g.OO  A.M. 
3.0O       " 
3.00       " 

9.00     " 

i3g 
140 
MI 
141 

26.5 
28.0 
27.0 
27.0 

107 

"4 

log 
109 

I5h.  56111. 
4h.   l6m. 
5h.  42m. 
nh.  4om. 

25(>97 
7  212 
8955 
18  2go 

21 

39 

28 

22 

Agitated    surface    of  sand 
layer  at  9.31  A.M. 
[layer  at  4.30  P.M. 
Agitated    surface    of  san^ 

162 


WATER  PURIFICATION  AT  LOUISVILLE. 

TABLE  No.  4. — Continued. 
Jewell  System. 


Rate  of 

j 

% 

0 

Collected. 

Filtration. 

JJ 

c 

'_S 

b. 

Period  of 

^  "S 

3  ^. 

A 

z 

Date. 

Hour. 

Number 

L   3 
O   C 

i  a 

^  t  5 
§*  = 

I 

Service  Since 
Last 
Washing. 

Hours  and 
Minutes. 

«  ^^- 

Sll 

"su 

R1 
iu 

Remarks. 

•c 

|i 

—    Q.  "* 

1 

-2 

CQ 

</> 

u 

i 

_] 

fc. 

1896 

2857 

May  12 

3.OO  A.M. 

142 

7.0 

109 

ih.  33m. 

2  566 

25 

2867 

"      12 

9.  oo     " 

142 

7.0 

109 

7h.  33m. 

12  196 

54 

2873 

"      12 

12.00  M. 

142 

7.0 

109 

loh.  3im. 

1  6  796 

22 

Agitated    surface    of   sand 

2877 

"       12 

8.30  r.M. 

143 

3-0 

93 

4h.  lorn. 

6  711 

19 

layer  at  10.26  A.M. 

2881 

"       13 

2.OO.  A*I. 

143 

7.0 

.109. 

-  .  . 

,  gh.  jSm. 

1  5'  30  1- 

^2 

Agitated    surface    of  sand 

2885 

'       13 

-  *?.'od   '" 

143,- 

6.  f. 

I0> 

.>  . 

I5h.  3$m. 

25031, 

12 

layer  at  1.38  A.M. 

2891 

'       13 

l.OO  Ml. 

M4> 

7.0 

H?9   '•  •}•  - 

3h.  i.2m. 

?4S3P 

H 

2896 

'       13 

7.0<i      " 

144.;. 

7-P 

id<) 

gh.  2im. 

1491^      13 

Agitated    surface   of   sand 

2900 

'       14 

.     .   ..     3.00,  A.M. 

M5 

7.0 

109 

4801. 

1258 

JO 

layer  at  5.15  r.M. 

2905 

'       14 

-      9.06  'V. 

M5- 

7.0 

109 

6h,  48m. 

io'Si8 

4 

2909 

'       14 

2.08  P.M. 

M5 

6.0 

105 

iih.  54m. 

19118 

37 

Agitated    surface    of    sand 

291-1 

'       M 

8.00     " 

M5 

7.0 

109 

I7h.  46m. 

28  748 

So 

layer  at  2.02  I'.M. 

2919 

'       15 

l.OO  A.M. 

146 

7.0 

109  j  

4h.  O2m. 

6430 

16 

2923 

'       15 

S.oo     " 

I4f> 

7.0 

109 

i  ih.  O2m. 

17640 

16 

2927 

'       15 

I  l.OO        " 

146 

7.0 

109 

I4h.  oom. 

23  340 

52    Agitated    surface    of    sand 

2932 

'       15 

5.15    P.M. 

"47 

6-5 

107 

3h.  14™. 

5  1  20 

M 

layer  at  9.09  A.M. 

2961 

'       '5 

I  1  .  OO       " 

'47 

7.0 

109 

8h.  5gm. 

14  280 

''5 

2970 

"     16 

5.00  A.M. 

147 

6-5 

107 

I4h.  57rn. 

24  O2O 

28 

Agitated    surface    of    sand 

2981 

"     16 

IO.OO       " 

148 

5.<> 

IOI 

5S,n. 

I  700 

19 

layer  at  4.35  A.M. 

2991 

"     16 

3.OO  P.M. 

148 

6.0    105 

gh.  58111. 

9  610 

15 

2999 

"     18 

I.I7       " 

'49 

25.0    ioi 

1.4 

05111. 

215 

1  08 

3000 

"     18 

1.27       ' 

"49 

25.0    ioi 

1-5 

i  5111. 

435 

4" 

3002 

"      18 

3.00      " 

149 

24.8 

100 

I  .( 

ih.  48111. 

2805 

91 

3008 

"      18 

6.05      " 

'49 

24-5 

99 

3-< 

4h.  53111. 

7  355 

192 

3010 

"      18 

9.00      " 

149 

25.0 

IOI 

3-3 

7h.  4801. 

ii  695 

3015 

"      18 

12.  OO        " 

149 

25.0 

IOI 

4.0 

loh.  48111. 

16145 

34 

3018 

"      19 

3.OO  A.M. 

149 

25.0 

IOI 

5-4 

I3h.  48m.    20655 

57 

3024 

'      19 

6.OO       '  ' 

149 

25.0 

101 

6.0 

i6h.  48m.  ,  25  155 

5i 

3027 

'      19 

8.30       " 

'49 

25.0 

IOI 

7.0 

igh.  I3m.  |  28  845 

26 

3032 

'      19 

12.OO  M. 

M9 

24-5 

99 

8.8 

22h.  48111.    34  085 

65 

[layer  at  2.22  P.M. 

3036 

'      19 

3.OO  I'.M. 

149 

25.0 

IOI 

6.0 

25h.  45m.    38  355 

43 

Agitated    surface    of    sand 

3041 

'      19 

6.00     " 

149 

25.0 

IOI 

8.2 

28h.  45m.  142  885 

37                  [layer  at  10.38  P.M. 

3044 

'      19 

g.oo     " 

149 

25-5 

103 

9.2    2ih.  45111.    47345     3'5    Agitated    surface    of    sand 

3050 

"       20 

l.OO  A.M. 

150 

26.0 

105 

05111. 

112 

!92    D.   Application    of  chemi- 

3051 

"        2O 

I.  10       " 

150 

25.0    101 

1-3 

15111. 

372       99 

D.      cals  unsatisfactory  on 

3053 

"       20 

3.00     " 

150 

25.0    ioi 

1.9 

2h.  05111. 

3082 

79 

D.       run   No.    150;    chem- 

3057 

"       2O 

6.00      " 

'5' 

25.  oj    ioi 

1.7             3im. 

77° 

(>5 

ical  feed-pipe  broken. 

3060 

"       2O 

8.30    " 

15" 

25.0 

IOI 

2.  I 

3)1.  oim. 

4480 

32 

3069 

"       2O 

12.00  M. 

151 

25.0 

IOI 

3.3 

6h.  31111. 

973° 

57 

3072 

"       20 

T.OO    I'.M. 

151 

25.0 

101 

5-4 

gli.  3  1  in. 

14  150 

30 

3077 

"       2O 

O.oo      " 

'51 

25.0 

H)l         O.I 

I2h.  3im. 

18620 

56 

3082 

"       2O 

9.  oo     " 

'5i 

25.0 

IOI 

8.3 

15!!.  31111. 

23050 

41 

[layer  at  II.  II  I'.M. 

3o8( 

"       20 

1  2  .  OO       " 

151 

25.0 

IOI 

5-9 

i8h.  2gm. 

27  260 

48 

Agitated    surface    of    sand 

308  c 

"       2 

3.OO  A.M. 

151 

24.0 

97 

9-3 

2ih.  2gm. 

31  760 

62 

Agitated  surf.S.L.,4.3iA.M. 

3093 

"       2 

6.00     " 

151 

23-5 

95 

g.( 

24!!.  27111. 

35940 

73 

Agitated    surface    of   sand 

3°95 

"       2 

7.54    " 

152 

25.5 

103 

2.3 

05111. 

109 

231 

layer  at  6.  16  A.M. 

3096 

"       2                                      8.04       " 

152 

25.5 

103 

1.6 

15111. 

379 

118 

309 

"       2 

8.30    " 

152 

25.5 

103 

i.t 

4im. 

939 

60 

310 

"       21 

I2.OO  M. 

152 

25.  c 

IOI 

2.7 

4)1.  1  1  in. 

6  28c 

65 

310 

"       21 

3.00  r.M. 

152 

24.5 

99 

7h.  i  im 

10889 

69 

3" 

"       21 

6.00     " 

152 

25.0 

IOI 

4-: 

i  oh.  inn 

I53I9 

69 

31' 

"       21 

9.00     " 

152 

25.  c 

IOI 

6.1 

I3h.  iim.    ig  759 

47 

3» 

"       21 

12.  OO       " 

152 

25.0 

IOI 

8.1 

i6h.  urn.    24229 

73 

312 
312 

"       22 
"       22 

3.00     " 
6.  oo     " 

152 
152 

23.5 
25.1 

T95 

101 

g.f 
g.c 

igh.  nm.    28  639 
22h.  ogm.    32  981, 

72 
gS 

[layer  at  3.21  A.M. 
Agitated    surface    of   sand 

313 

"       22 

8.30    " 

152 

24.  c 

97 

g.f 

24h.  37m.    36  55C 

88 

Agitated    surface    of    sand 

3'3 

!                 "       22 

10.24     " 

'53 

25.  c 

IOI 

i.f 

05  m 

I3C 

87 

layer  at  7.2ijA.M. 

313 

"       22 

11.34    " 

153 

24.  c 

97 

I.' 

1501.         37^ 

99 

3'3 

7                 "       22 

12  00  M. 

'53 

25.  c 

IOI 

2.( 

>      ih.  4im.      2  581 

66 

3M 

2                 "       22 

3.00  r.M. 

153 

24  •! 

99 

3-< 

)      4h.  4im.      7031. 

39 

3M 

315 
IIS 

i                 "       22 
"       22 
.                 «       22 

6.  oo     " 
9.00     " 

I2.OO       " 

153 
'53 
1^3 

25. 

25.  c 
25.  < 

103 
IOI 
101 

4- 
6. 
4- 

7h.  41111.    II  56t 
loh.  4im.    15  97C 
>    13(1.  39m.1  20  341 

61 
41 
98 

[layer  at  11.54  I'.M. 
Agitated    surface    of    sand 

COMPOSITION  OF  OHIO   RIVER    WATER   AFTER   PURIFICATION. 


•  6.5 


TABLE  No.  4. — Continued. 

Jewell  System. 


Rate  of          C 

« 

Collected. 

Filtration. 

£ 

B 

.S 

J 

~t 

Ul    u 

Period  of 

u  <* 

3 

£ 

Number 

c. 

o  a 

"S 

ServiceSince 
Last 

Sf  s 

^fe 

S 

3 

Date. 

Hour. 

Run. 

!l 

'|l| 

= 

Washing. 

Hours  and 
Minutes. 

»-  *  A     '      V  G 

Kc-m;.rks. 

.2 

is 

i  £."? 

si 

—  .JCJ        5^U 

X 

u 

S 

J 

£ 

m 

1896 

3164        May    23 

g.iS  A.M. 

154 

55-° 

222 

6.0 

o8m. 

4^7       35 

D.     Run    No.    154    was    a 

3165           "      23 

9.28     " 

'54 

55.0 

222 

6.0 

iSrn. 

957      23 

F>.           special    run    at    the 

3166:           '       23 

9-3S     " 

'54 

55-° 

222 

6.0 

28111. 

I  447       26 

D.            request     of      Filter 

3i&7!           '      23 

10.08     " 

'54 

2'4 

6.0 

5Sm. 

2977       31 

I).           Company. 

3168            '       23 

10.38     " 

'54 

50.0 

2O  2 

6.1 

ih.  28m. 

6617       27 

D. 

3175!           '       25 

12.00  M. 

'55 

29.5 

120 

2  .  7 

ih.  4gm. 

3322 

74 

3178:           '       25 

2.OO  P.M. 

'55 

29.0 

118 

4.0 

3h.  49111. 

6  832      43 

3182            '      25 

6.OO       " 

155      3°-° 

122 

5-' 

7(1.  4gm. 

14  132!      28 

3185;           '      25 

8.00       " 

155      30.0 

122        6.5 

gh.  49'^- 

17932        21 

3189            '      25 

12.  OO       " 

155 

30.0 

122 

5-1 

I3h.  47m 

24842 

34 

Ag  tated    surface    of    sand 

3192            '      26 

2.00  A.M. 

155      30.0 

122 

6.5 

I5h.  47m. 

28362 

34 

aver  at  1  1.09  p  M. 

3  i  98            '      26 

6.0O       " 

155      29.0 

IlS 

4.4 

igh.  45m. 

35  172 

35     Agitated    surface    of    sand 

3200          '  '      26 

7-39       " 

156      29.0 

US 

1.8 

05m. 

133 

"4 

layer  at  5.06  A.M. 

3201 

'       26 

7-49     " 

156 

30.0 

122 

I.  g 

I5'». 

413 

76 

3203 

"       26 

8.30    " 

156      30.0 

122 

2.1 

56m. 

i  643    134 

3209                   26 

IO.OO       " 

156      30.0 

122 

2.S 

2h    26m. 

4313      25 

3213             "        2f> 

2.00  P.M. 

156     130.0 

122 

5.0 

6h.  26m. 

1  1  533      34 

3216              '        26 

4.00     " 

156    ;3o.o 

122 

6.5 

Sh.  26111. 

15703      46 

3222             "        26 

S.co     " 

156     30.0 

122 

5-5 

I2h.  24tn. 

22  543  .    5° 

Agitated    surface    of    sand 

3225!             "         26 

10.00     " 

156     j3o.o 

122 

I4h.  24111. 

26  143      52 

layer  at  6.20  P.M. 

3229                '         27 

2.OO  A.M. 

156      30.0 

122 

7-5 

iSh.  22111. 

32  883'     46 

Agitated    surface    of    sand 

3233;               '         27 

5.1°     " 

'57      25.0 

I  01 

1.8 

i  im. 

130      81 

layer  at  11.58  P.M. 

3234|               '         27 

5.20     " 

157 

30.0 

122 

2.  1 

2im. 

49°      73 

3237                '         27 

7.3°     " 

157     t3°-° 

122 

3-1 

2h.  3im. 

4480      46 

324I1               '        27 

12.00  M. 

157      3°-° 

122 

6.0 

7h.  oim. 

I  2  670 

135 

flayer  at  2.14  P.M. 

3246                '         27 

3.00    P.M. 

'57      29.0 

118 

5-1 

gh.  5gm. 

1771° 

30 

Agitated    surface    of    sand 

3256;             "         27 

6.OO       " 

'57 

30.0 

122 

6.9 

I2h.  59111. 

22  980 

34 

Agitated    surface    of    sand 

326i:             "         27 

9  20      " 

.58 

30.0 

122 

2.0 

05111. 

182 

206 

layer  at  7.13  P.M. 

3262              "        27 

9.3°    " 

158 

30.0 

122 

2.0 

15111. 

422 

152 

3265              "         27 

12  00       " 

158       30.0 

122 

3-3 

2h.  45111. 

4982 

57 

3267              "         28 

3.OO  A.M. 

158     J3O.O 

122 

7.' 

5h.  45'"- 

10  342 

51 

Agitated    surface    of    sand 

3273              "         28 

6.00       " 

158      30.0 

122 

5-9 

Sh.  43m. 

15  702 

47 

layer  at  3.11  A.M. 

3276                '         28 

7.30       " 

158      30.0 

122 

7-3 

loh.  13111. 

18362 

43 

Ag  tated    surface    of    sand 

3280              "         28 

10.00 

158       29.5 

I  2O 

7.0 

I2h.  41111. 

22  4O2 

54 

layer  at  7.51  A.M. 

3283              "         28 

11.00       " 

159      29.5 

120 

1.9 

05111. 

157 

246 

3284              "         28 

1  1  .  20     " 

159       29.0 

I  2O 

2.0 

lem. 

447 

158 

3295          "      28 

2.OO    P.M. 

159 

30.0 

122 

2.g 

2h.  55111. 

5  177 

162 

3298           '      28 

4.OO       " 

159 

30.0 

122 

4-2 

4h.  55tn. 

8737 

300 

3306          "      28 

S  .  oo      " 

160 

30.0 

122 

2.7 

2h.  30111. 

4497 

423 

I). 

3310           '      28 

9-35     " 

I()i       3°.° 

122 

2.O 

05111. 

193 

668 

1). 

3311          "      28 

9-45      ' 

1  61       130.0 

122 

2.O 

15111. 

443 

560 

1). 

3312 

••       28 

9.58   ;; 

161      30  .  o 

122 

2  .O 

28m. 

833 

650 

t).          Prescribed     amount 

3316 

"       28 

162     po.o 

122 

1.  9 

05111. 

157 

460 

I).  <-          of    chemicals    in- 

i   i-jn 

"       28 

11.25       " 

162 

30.0 

122 

2.0 

13111. 

337 

345 

1).              sufficient. 

3326 

"       29 

12.5(1  A.M. 

163 

30.0 

122 

2.0 

05111. 

165 

715 

i). 

333" 

'       29 

1.  06    " 

163 

30.0 

122 

2.1 

15111. 

435 

394 

I). 

3333 

'       29 

2.00       " 

163 

30.0 

122 

2.3 

ih.  09111. 

2  065 

510 

D.J 

334° 

'       29 

4.00     " 

163 

30.0 

i  2  • 

4.8 

3h.  ogm. 

5625 

3f>3 

3342 

'       29 

4.35    " 

163 

30.0 

122 

5.7 

3h.  44m. 

6635 

2/5 

3346 

'       29 

5-59     " 

164 

2S.O 

"4 

2.1 

05  m. 

293 

151 

3348 

2g 

6.09     " 

164 

24.0 

97 

2.2 

15111. 

473 

149 

'      29 

7.30     " 

164 

25.O 

tor 

2.2 

ih.  36111. 

2523 

So 

33"! 

'       29 

12.05    P.M. 

,65 

29-5 

120 

2-5 

45111. 

875 

212 

3364 

'      29 

2.OO       " 

1  66 

29.5 

120 

3-  r 

ih.  oom. 

1888 

I2g 

,368 

'      29 

6.00       " 

169 

3O.O 

122 

2.0 

28m. 

954 

465 

3375 

'       29 

S.lg       " 

171 

30.0 

122 

2.1 

1  5  m  . 

493 

118 

3380 

'      3° 

12.27  A.M. 

174 

2O.  O 

Si 

I  .1 

15111. 

344 

128 

3384 

'      3° 

2.OO      " 

'74 

20.  0 

Si 

1-5 

ih.  48111. 

2184 

222 

3388 

'      3° 

6.26      " 

175 

29-5 

120 

2.1 

2bm. 

720 

415 

3394 

'      3° 

8.00     " 

176 

29.5 

1  20 

2.1|                   I4IT). 

402 

275 

34°° 
34°' 

'      3° 
"      30 

10.15     " 

12.00  M. 

'77 
178 

30.0 

30.0 

122 
122 

2.2J            3om. 
2.1             28m. 

9°3 
863 

475 
169 

Agitated    surface    of    sand 

3434       June     2 

3.50   P.M. 

'79      34-0 

3.3!                  2.1111. 

I   .1"!  1    2*.) 

layer  at  3.27  P.M. 

1 64 


WATER  PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  4. — Continued. 

Jewell  System. 


Rate  of 

ti 

0 

Collected. 

Filtration. 

£ 

t/5   •         j5 

Ji 

Number 

s. 

jg. 

I'enocl  ol 

O/J                3 
«•£.;          <J     . 

X! 

E 
^ 

Run. 

t.  ~ 

lf| 

s 

l.ast 
Washing 
Hours  and 

*|£            £S 

Remarks 

Date. 

Hour. 

3 

0  ^1 

Minutes. 

y.y.'2 

a  S 

•£ 

.r.  -- 

=  g.  J 

1 

-25 

^$ 

in 

u     j  S 

t.       ;  « 

I  S()6 

I 

3436 

June     2 

4.37    P.M. 

179 

34-5     MO 

4.0 

ih.  1  6m. 

2  701      62O 

3439 

2 

6.20        " 

181 

20.  5 

83 

2.1                     IJIll. 

410     191 

3442 

"          2 

10.37        " 

182 

27.0    109 

5.1      2li.  25m. 

3  989        22 

3447 

3 

3.30   A    11. 

183 

25.0    IOI 

3.1      2h.  56111. 

4  448       36 

3451                      3                          6  oo     " 

184 

25.0    TOI 

2-7 

3im. 

745      44 

345-1                      3                          9-^0     " 

184 

25.0 

IOI 

.  .  .  .       3h.  31111. 

5  345       26 

3458 

3 

T2.OO  M. 

184 

25.  o     lot 

6.7      6h.  26111. 

434       25 

3460 

3 

2.00    P.M. 

184 

20.0         8  1 

9.5       Sh.  13111. 

2  145       50    Agitated    surface    of    sand 

3464 

3 

4.30       " 

185 

24-5      99 

2.  5      2)1.  lorn.      3  356      70 

layer  at  I  06  P.M. 

3468 

3 

6.00     " 

185 

25.0    101 

3.4       3)1.  40111. 

5  526     144 

3472 

3 

9  oo     " 

1  86 

25.0 

IOI 

2.0         ill.    21  ID. 

2  06  1       1  6 

3478 

3 

12.00        " 

1  86 

25.0    101 

4  .6      4)1.  2  1  m. 

6451       36 

[layer  at  1.41  A.M. 

3482 

4 

3.00  A.M. 

1  86 

25.0    ioi 

8.5      7(1.  1401.    10741       36    Agitated    surface    of    sand 

34S4 

4 

3.30       " 

186 

21.0        85 

7h.  44m.    11451       64   JShut   inlet    3.27  P.M.,   out- 

3487 

4 

6.00     " 

187 

25.0 

IOI 

2.  I 

2h.  07m.      3  198      43 

let  3.38  P.M. 

3  49- 

'  '        4 

9  oo     '  ' 

187 

5h.  07111  .     7  ^88      JT 

3496 

4 

10.37     " 

187 

25-5 

103 

7.0 

fth.  44'"- 

9  948       54 

3498 

4 

12.02    P.M. 

187 

23.0 

93 

9.7      8b.  (xjm. 

11978:     38 

3501 

4 

3-43       " 

.89 

25.0 

IOI 

1-7 

2im 

851       24 

3506 

4 

6.05      " 

189 

25.0 

IOI 

2.4      2h.  53m. 

4611     1  1  6 

3509 

4 

8.40     " 

190 

25.0 

IOI 

2.1 

2ll.    12111. 

3  422      61 

3511 

4 

9-55     " 

190 

25.0 

IOI 

3.2      3)1.  27111. 

5442      71 

Shut    inlet   9.53    P.M.,  out 

3512 

4 

10.22       " 

191 

25.0 

IOI 

•  7 

02111. 

50      78 

let  10.01   P.M. 

3513 

4 

10.24       " 

191 

25.0 

IOI 

.7 

O4in. 

loo      44 

3514 

4 

IO.26       " 

191       27.5 

III 

.7 

o6m. 

155 

35 

3515 

4 

10.28       " 

191       27.5 

1  11 

•  7 

08111. 

210'     33 

3516 

4 

10.30      " 

191       25.0 

IOI 

•  7 

I  om  . 

260        22 

3517 

4 

10.32       " 

191 

25.0 

IOI 

.  7 

12111. 

310     29 

35i*> 

4 

10.34       " 

191 

27.0 

C9 

•  7 

14111. 

365       33 

3519 

4 

10.36       " 

191 

25.0 

01 

7 

16111. 

415      23 

3520 

4 

10.38       " 

191 

27.0 

09 

•  7 

iSm. 

470      27 

3521 

4 

10.40       " 

191 

2J.O          01 

.7 

20111. 

520      43 

3522 

4 

10.42       " 

191 

27.0       09 

.7 

22II1. 

575       10 

3523 

4 

10.44       " 

191 

27.0       09 

•  7 

24111. 

630  ;      15 

3524 

4 

10.46       " 

191 

25.0      01 

26m. 

680      87 

3525 

4 

10.48       " 

191 

25.0      ol 

.7 

28m. 

73°;      99 

3526                      4 

10.50       " 

191 

25.0      01 

.7 

30111. 

780       II 

3527                      4 

I0.;2       " 

191 

25.0      o; 

.7 

32111. 

830 

114 

35281                     4 

10-55      ' 

191 

25.  O;            Ol 

.7 

35111. 

910 

17 

352')                       4 

1.05      ' 

191 

25.0     oi 

•  7 

45111. 

I  160 

16 

3530                     4 

1.  20     " 

191 

25.0    ioi 

.i> 

ih.  oom. 

I  540 

25 

353'                      4 

1.50      " 

191 

23.0     ioi 

2.O 

ih.  3»»i. 

2350 

52 

353? 

5 

2.  2O  A.M. 

191 

25.0    ioi 

2.1 

2)1.  oom. 

3  100 

27 

353h 

5 

2.50 

191 

25.0    ioi 

2.  I 

2ll.    30111. 

3  870 

46 

3537 

"        5 

1  .  2O        " 

191 

25.0!   ioi 

2.2 

3h.  oom. 

4  620 

33 

3539 

5 

3-22        " 

192 

30.0     122 

2-3 

ih.  O2m 

I  848 

18 

3543 
3556 

I        I 

6.  co      " 
4-55  I'.M. 

192 

197 

29-5 

35-0 

1  20 

142 

3-9 

2.5 

3h.  40111. 
35m. 

6  528 
I  134 

94 

Si 

3559 

5 

IO.OO       " 

200 

30.0 

132 

2.1 

5"m. 

I  5'9 

7 

35«f 

6 

2.30  A  M. 

2OI 

25.0 

101 

2.  I 

2ll.    I  2111. 

3386 

9 

3596 

6 

7.48       " 

2O3 

25.0 

IOI 

1.7 

53"i- 

I  312 

14 

3624 

6 

10.55       " 

203 

25.0 

101 

2.f 

4h    oom. 

5992 

29 

3629 

"       6 

1.55    I'-M. 

204 

34-5 

140 

2-9 

ih.  03111. 

2016 

14 

3f>32 

"       6 

3-00       " 

204        33-5 

136 

3-1 

2h.  oSm. 

4116 

12 

3657 

"       9 

I2.5O       " 

2O5        25.C 

IOI 

2.  I 

ill.  54111. 

2854 

170 

3661. 

9 

5.0O       " 

2O6 

25.  C 

IOI 

I  .9 

ih.  22m. 

2074 

39 

3669 

"       o 

11.15  A  M. 

2O7       '25.  t 

IOI 

I.( 

56111. 

I  415 

II   '.  Agitated    suiface    of    sand 

3672 

"         0 

I.  CO    P.M. 

207      25.  c 

IOI 

2.C 

2h.  4im 

4045 

9 

layer  at  10.06  A.M. 

3&7« 

"      o 

330       " 

2O7         25.  L 

IOI 

5.2 

4)1.  1  1  in 

6925 

13 

3682 

"      I 

IO.32  A.M. 

207         25.( 

IOI 

5-7 

8h.  41111. 

12945 

14 

3685 

"      I 

1.  00    I1  M. 

208 

25  .c 

IOI 

I  .7 

25111 

644 

7 

3693 

"     II 

3.42       " 

208      25.  c 

IOI 

2.f 

3h.  O7m. 

4  804 

ib 

3699                '       12                            II.  II   A  M.                           209       25.0     IOI 

I  .7 

3im. 

704         9 

COMPOSITION  OF  Off  TO   RIVER    WATER  AFTER   PURIFICATION. 

TABLE  No.  4. — Continued. 
Jewell  System. 


165 


Rate  of 

J 

Collected. 

Filtration. 

fc 

£ 

1 

Number 

S. 

f  s. 

-d 

Period  of 
Service  Since 
Last 

be 

U  j 

e 

Remarks. 

3 

Run. 

v  ri 

O  5  5 

S 

Washing. 

>£h 

^"c 

7. 

Date. 

Hour. 

ol 

JjE 

Minutes. 

al 

!i 

i 

U 

~  a  cT 

A 

J 

£ 

!u 

1896 

3703 

June  12 

1.38   P.M. 

209 

25.0 

IOI 

2-3 

2h.  sSm. 

4474 

12 

3706 

"       12 

2.48   " 

209 

25.O 

IOI 

2.8 

4h.  ogtn. 

6  184 

12 

37'3 

"     '3 

II.  O2  A.M. 

210 

25.0 

IOI 

1-5 

22m. 

485 

23 

37'9j            '      '3 

I.OO   P.M. 

210 

25.0 

IOI 

2.1 

2h.  2Om. 

3585 

15 

37251            '      '3 

2.55    " 

210 

25.0 

IOI 

2.7 

4h.  ism. 

6465 

51 

3728 

'     13 

5.02       " 

210 

25.0 

IOI 

4-3 

6n.  I2m. 

9335 

7' 

•17-37 

"     r  5 

9  .  (X)      " 

2  IO 

6h.  4Om. 

IO  I  28 

1153 

B.  Collected    before   the 

J  1  J  1 

3741 

"     15 

10.15  A.M. 

211 

25.0 

IOI 

1-7 

5om. 

i  248 

IO 

filter  was  in  opera 

3744 

'      '5 

12.23    P.M. 

211 

25.0 

IOI 

2-7 

2h.  5801. 

4484 

25 

tion    and  after    pe 

3748 

'     15 

3.02       " 

212 

25.0 

101 

37m. 

i  005 

19 

riod    of    rest  of    39 

3754 

'     15 

4.31       " 

212 

25  o 

IOI 

2.  I 

2h.  o6m. 

3355 

II 

hours  30  minutes. 

376o 

"      16 

10.25  A.M. 

213 

38.0 

154 

3-7 

3801. 

i  429 

9 

3764 

"     16 

12.38    P.M. 

214 

38.0 

154 

3-1 

32111. 

i  27&I         5 

3797 

"     18 

10.10  A.M. 

216 

25.0 

IOI 

i  .7 

ih.  0701. 

i  7i8!       28 

3802 
3810 

"     18 

"     18 

12.34    P.M. 

2-49       " 

2l6 
216 

25.0 
25.0 

IOI 
IOI 

3-' 
5-0 

3h.  3im. 
5h.  46111. 

5398        15 
8678          8 

3815 

18 

4-55       ' 

216 

25.0 

101 

7-4 

7h.  47m. 

11678        28 

[layer  at  11.23  A  M. 

3819 

"    19 

10.00  A.M. 

216 

25.0 

IOI 

7-9 

cjh.  22m. 

14118        39  Agitated  surface  of  sand 

3825 

"        IO 

12.56  P.M. 

216 

1  2h.  1  3m. 

18346           lo  Shut  outlet    12.  =;6  P.M. 

3830 

1  V 

'  19 

2.59     " 

217 

25.0 

IOI 

1.8 

45m. 

I  072 

69 

3846 

'  19 

4.32     " 

217 

25.0 

101 

i.S 

2h.  i8m. 

3422 

"4 

3860 

"       20 

11.33  A.M. 

218 

25.0 

IOI 

1.6 

38m. 

976 

"7 

3863 

"      20 

12.43    P.M. 

218 

25.5 

103 

'•7 

ih.  48m. 

2  7l6 

69 

3872 

"      20 

3-42       " 

219 

25.0 

ioi      1.6 

25m. 

638 

88 

3875 

"       20 

4.38       " 

219 

25.  o 

ioi      1.6 

ih.  2im. 

2038 

IOI 

"       22 

9-OO  A.M. 

0  IO 

69 

B.Coll.  before  fikerwas  in  oper 

3889 

22 

10.15    " 

-  '  y 

219 

25.0     IOI    !    2.0 

3h.  28m. 

5258 

74 

ation  and  after  rest  of  39(1.3010. 

3891 

"       22 

12.25    P.M. 

5h.  3801. 

8  538 

300 

A.   Shut  inlet  12.21  P.M., 

3895 

"       22 

I.  IS     " 

2  21 

25.0    ioi 

1.6 

23m. 

533 

96 

outlet  12.31  P.M. 

3900 

"       22 

3.01      " 

2  21 

25.  0:    101        2.  1 

2h.  o6m. 

3213 

79 

3904 

"       22 

5.cx)      " 

221 

25.0     ioi 

2.6 

4h.  O5m.     6243 

97 

3910 

23 

9.52  A.M. 

22C 

5h.  2501. 

8275 

Shut  outlet  9.52  A.M. 

3925 

"       23 

11.12       " 

22 

25  .  o 

loi         l.S 

5Sm. 

1438 

216 

3927 

"     23 

1.30  P.M. 

22 

25.0 

IOI         2.  I 

3h.  i6m. 

49'8 

393' 

"     23 

3.20       " 

22 

25.0 

ioi       1.7 

5h.  o6m. 

7688 

62 

3934 

"      23 

4.42       " 

22 

6h.  2Sm. 

9  759 

77 

Shut  outlet  4.42  P.M. 

3939 

"      24 

10.  17  A.M. 

222 

25.0 

ioi       1.8 

ih.  33m. 

2389 

840 

3948 

'  '       24 

12-39  P-M. 

222 

3  1  1  .  55m. 

f,   946 

470 

Shut  outlet  12.39  P.M. 

395' 

"      24 

'•34      " 

223 

25.0 

ioi       1.6 

38m. 

793 

385 

3955 

"    24 

3-24      ' 

223 

25.0 

IOI 

1.8 

2h.  28m. 

3643 

355 

3965 

"      24 

4-5'      ' 

223 

25.9 

IOI 

2.  I 

3h.  55m. 

5753 

215 

3979 

"     25 

9.50  A.M. 

224 

25.0 

IOI 

1.4 

03  in. 

93 

45 

3980 

"    25 

9-55      ' 

224 

25.0 

loi 

1.4 

08  m. 

223 

398' 

"     25 

0.<X)        " 

224 

26.0 

105         1.4 

I3m. 

353 

3982 

"      25 

0.05    •' 

224 

25.0    ioi       1.4 

i8m. 

483 

57 

=•,-; 

"     25 

0.  IO        " 

224 

25  o    ioi      1.5 

2301. 

613 

2'5 

3984 

"    25 

0.15    " 

224 

25.0!   ioi      1.5 

28m. 

733 

515 

3985 

"     25 

0.20       " 

224 

25.0    ioi       1.6 

33m. 

863 

i  750 

19-7 

"     25 

0.25      " 

224 

25.  oj   ioi       1.6 

38m. 

983 

362 

vr- 

"    25 

0.30   " 

224 

25.0    ioi       1.6 

43m. 

103 

i  780 

399' 

"     25 

"•35      ' 

224 

25.0    ioi 

1.6 

48m. 

233 

215 

3992 

"    25 

0.40      " 

224 

25.0    ioi 

1.6 

5301. 

353 

445 

3993 

"    25 

0.45      ' 

224 

25.0    ioi       1.6 

58m. 

473 

95" 

3994 

"     25 

0.50      " 

224 

26.0    105 

1-7 

ih.  0301. 

613 

249 

3995 

"     25 

1.05      ' 

224 

25.0!   ioi 

ih.  i8m. 

983 

420 

3996 

"    25 

1.20       " 

224 

25.  o!   ioi       1.7 

ih.  33m. 

2373 

99° 

3997 

"     25 

'•35     " 

224 

25.0    ioi      1.7 

ih.  48m. 

2753 

395 

3998 

"    25 

1.5"     " 

224 

25.0    ioi      1.9 

2h.  03m. 

3163 

900 

3999 

"    25 

2.O5    P.M. 

224 

25.0'    ioi       1.9 

2h.  iSm. 

3523 

365 

4<J02 

"    25 

I.I5       " 

225 

25.0 

ioi      1.7 

46m. 

I  166 

510 

4<x>5 

"      25 

231       " 

225 

°h    o°m 

3  060 

250 

Shut  outlet  2.31  P.M. 

4  cxx; 

"    25 
"    25 

3.16       " 
4.25       ' 

226 
226 

25.0 

ioi      1.4 

1  3m. 
ih.  22m. 

236 
2091 

600 
173' 

Shut  outlet  4.25  P.M. 

1 66 


WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  4. — Continued. 
Jewell  System. 


Rate  of 

S 

8 

Collected. 

Filtration. 

£ 

£ 

2 

t 

Number      % 

Is. 

•6 

Period  of 
Service  Since 

S.S  j 

3 
U  ^ 

g 

Run. 

t   . 

*££ 

I 

Last 

Washing. 

£££ 

£1; 

Remarks. 

X 

Date. 

Hour 

b  ~ 

<  0 

_ 

Hours  and 

•a£  u 

•-•! 

— 

o  c 

o  ,_  -C 

° 

Minutes. 

S  M  ja 

u  c 

c 

15 

=  S  J 

| 

^23 

<J(J 

c/i 

o 

K  ~ 

" 

£ 

B 

1896 

4013 

June  25 

5.00  P.M. 

227 

25.0 

IOI 

1-5 

iSm. 

465 

347 

4024 

"      26 

10.27  A.M. 

227 

25.0 

101 

1.8 

2h.  I4m. 

3235 

23 

4O2S 

"      26 

11.40       '  ' 

•72*7 

3h    27m. 

5  204 

6  1 

Shut    inlet     11.37    A.M. 

4031 

"      26 

I.I4   P.M. 

228 

25.0 

IOI 

1.9 

ih.  i6m. 

I  g2i 

19 

outlet  11.47  A.M. 

4034 

"      26 

2-35       " 

228 

2h.  37m. 

4  026 

79 

Outlet  closed  for  wash. 

4035 

"      26 

3-3"     " 

229 

25.0 

IOI 

2.0 

4om. 

I  005 

9 

4037 

"      26 

4.50     " 

229 

25.0 

IOI 

1.8 

2h.  oom. 

2g45 

29 

[wasting  at  end  of  run. 

4U42 

"      27 

0.2O  A.M. 

Waste.    Collected    after 

4044 

"      27 

IO.26       " 

230 

25.0 

IOI 

1.7 

32m. 

839 

44 

4048 

1  '      27 

12    IO  P  M 

2TO 

2h.  i6m  . 

3  425 

Shut     inlet     12.06    P.M. 

4052 

"     27 

1.58    " 

231 

25.0 

IOI 

1.  9 

ih.  2gm. 

2  194 

315 

outlet  12.  16  P.M. 

4<>55 

"    27 

3.20    " 

232 

25.0 

IOI 

!•  5 

I5m. 

441 

39 

4056 

•'    27 

4.46    " 

232 

25.0 

IOI 

i.  5 

ih.-  4im. 

2  551 

41 

4062 

"    29 

10.  16  A.M. 

233 

25.0 

IOI 

1-7 

36m. 

937 

4 

4064 

"    29 

11.49       " 

233 

25.0 

IOI 

2.  I 

2h.  ogm. 

3577 

6 

4068 

"    29 

1.28    P.M. 

233 

25.0 

IOI 

2.2 

3h.  48m. 

5787 

9 

4070 

"    29 

3.38       " 

233 

25.0 

IOI 

6.6 

5h.  58m. 

9  067 

II 

4»73 

"    29 

5.13       " 

233 

25.0 

IOI 

9.6 

7h.  33m. 

II  267 

9 

Agitated  surface  of  sand 

4082 

"    30 

10.  14  A.M. 

234 

25.0 

IOI 

1.8 

23m. 

630 

7 

layer  at  9.00  A.M. 

4100 

"    30 

12.45    P.M. 

234 

23.5 

95 

2.6 

2h.  54m. 

4  270 

5 

4105 

"    30 

2.52       " 

234 

23.5 

95 

6.1 

5h.  oim. 

7  290 

3 

4108 

"    30 

4.31        ' 

234 

23.5 

95 

4.1 

6h.  3im. 

9338 

4 

[layer  at  11.20  A.M. 

4114 

July 

IO.25  A.M. 

234 

23-5 

95 

o.o 

Sh.  53m. 

12  730 

* 

Agitated  surface  of  sand 

41  16 

11.25       " 

234 

21.0 

85 

1-4 

gh.  som. 

13942 

Wasting  i  min.,  locu.ft. 

4117 

11.28       " 

234 

21  .O 

85 

1.4 

gh.  som. 

13  942 

4     "     100     " 

4118 

11.31       " 

234 

21.  O 

85 

1.4 

gh.  som. 

13942 

7  '"      I5<J     " 

4H9 

"-34     ' 

234 

21.0 

85 

1.4 

gh.  Som. 

13942 



Opening  outlet. 

4120 

it.  37     " 

234 

22.0 

89 

1-4 

gh.  53111. 

14010  

4121 

1  1  .  40     " 

234 

23-5 

95 

1-5 

gh.  5501. 

14060  

4123 

" 

I.I7    P.M. 

234 

23.0 

93 

10.7 

ih.  32m. 

16080  

[layer  at  2.11  P.M. 

4125 

2.08       " 

234 

15.0 

61 

II.  2 

2h.  23m. 

16890  .'  

Agitated  surface  of  sand 

4126 

2.14       ". 

234 

15-0 

6  1 

8.7 

2h.  27m. 

16  937  

Starting  to  waste. 

4127 

2.16       " 

'      234 

16.0 

65 

g.o 

2h.  27m. 

16937 

Wasting  2  min..  45  cu.ft. 

4128 

2.18       " 

234 

18.0 

73 

9-5 

2h.  2701. 

16  937 

4     "        95      " 

4129 

2.22       " 

234 

18.0 

73 

9-5 

2h.  27m. 

16  937 

8     "      155      " 

4130 

2.27       " 

234 

17.0 

69 

g.6 

2h.  27111. 

if>  937 

Opening  outlet. 

4135 

4-34       ' 

235 

23-5 

95 

I  .  2 

39  m. 

951 

4144 

10.29  A.M. 

235 

23-5 

95 

2.  I 

3h.  oim. 

4  231 

49 

4148 

11.30       " 

235 

23-5 

95 

4h.  O2m. 

5  701 

3 

I  2.OO  M 

ih    i->m 

6406 

1  1  c 

4152 

12.35    P.M. 

235 
236 

23-5 

95 

I.  1 

4".   j-lll< 
urn. 

325 

M4 

4153 

1.04       " 

236 

23-5 

95 

I  .2 

40111. 

965 

in 

4157 

3.05       ' 

237 

23-5 

95 

1.6 

5om. 

1  155 

9 

4165 

"       3 

10.14  A.M. 

237 

23-5 

95 

6.2 

4h.  2gm. 

6  2g5 

0 

4170 

"       3 

12.15    P.M. 

3om. 

8  065 

2 

Shut  outlet  12.15  P.M. 

4173 

3 

12.50       " 

237 

238 

23-5 

95 

I.  2 

V     J 

114 

6 

4174 

3 

12.55       " 

238 

23.0 

93 

I.  2 

lorn. 

244 

10 

4175 

3 

I.OO       " 

238 

20.  o 

81 

1.3 

I5m. 

344 

I 

4176 

3 

1.05       " 

238 

22.0 

89 

t-4 

2om. 

454 

8 

4'77 

3 

I.IO       " 

238 

24.0 

97 

1.4 

25111. 

594 

15 

4179 

3 

1.  15     " 

238 

25.0 

IOI 

1-4 

3om. 

724 

IO 

4180 

3 

1.20       " 

238 

23.0 

93 

1-5 

35m. 

834 

13 

4181 

3 

1.25       " 

238 

24.0 

97 

1.6 

4om. 

954:       8 

4182 
4183 

3 
3 

I.3O       " 
1-35       " 

-     238 

238 

23.5 
24.0 

95 

1.6 

45m. 
5om. 

I  064        7 
I  194!     13 

4184 

3 

1.40       " 

238 

23-5 

95 

1.8 

55m. 

I  214        6 

4185 

"       3 

1.45     ' 

238 

23.5 

95 

1.8 

ih.  oom. 

I  344       1  1 

4188                     3 

2.00       " 

238 

23.0 

93 

1.8 

ih.  ism. 

I  794'      II 

4189!                   3 

2.15       " 

238 

23-5 

95 

1.8 

ih.  3om. 

2  164     125 

4'9°                    3 

2.30       " 

238 

2  5  .  5 

95 

1.8 

ih.  45m. 

2  504        8 

4191 

3 

2.45      ' 

238 

23.5 

95 

1.  9 

2h.  oom. 

2864        6 

4192 

3 

3.00     " 

238 

23.5 

95 

2.0 

2h.  I5m. 

3  204      24 

4193 

3 

3-1.5     " 

238 

23.5 

95 

2.1 

2h.  3om. 

3  574      M 

*  The  bacterial  results  of  July  I  were  lost  through  melting  of  the  culture  medium. 

COMPOSITION  OF  OHIO   RIVER    WATER  AFTER  PURIFICATION. 

TABLE  No.  4. — Continued. 
Jewell  System. 


,67 


Rate  of 

s 

{j 

Collected. 

Filtration. 

[i. 

y> 

.H 

. 

~^ 

'  ^ 

Period  of 

».  "« 

3 

1 

Number 

s. 

o  a 

•g 

Last 

^"1  ^ 

^  'Z 

E 

Run. 

OJ   U 

3  s  " 

X 

Washing. 

:£,"(£ 

O.U 

Remarks. 

'£. 

Date. 

Hour. 

'oi 

lu  = 

Hours  and 
Minutes. 

1*2 

|| 

•c 

Is 

=  8.  j 

1 

¥  J!J 

'•'cj 

X 

u 

s 

,4 

£ 

m 

1896 

4194 

July      3 

3.30  P.M. 

238 

23.5 

95 

2.2 

2h.  45m. 

3924 

16 

4229 

6 

3.27      " 

239 

23.5 

95 

37m. 

960      281 

42333 

6 

4.25      " 

239 

24.0 

97 

6.8J     ih.  3501. 

2  380     223 

4234 

"       6 

5.00     " 

239 

25.0 

IOI 

2.3      2h.  oSm. 

3  130:  357 

Agitated   surface   of   sand 

42343 

6 

5.03     " 

239 

25.0 

IOI 

2.5      2h.  i  im. 

3  210    362 

layer  at  4.53  P.M. 

4235 

6 

5.06     " 

239 

25.0 

IOI 

2.5      2h.  14111. 

3  280    372 

4236 

6 

5.09     " 

239 

25.0 

IOI 

2.7      2h.  I7m. 

3  340    399 

4237 

"       6 

5.12     ' 

239 

25.0 

IOI 

2.7j       2ll.    2Onl. 

3420!   393 

4238 

6 

5-15     " 

239 

25.0 

IOI 

2.8      2h.  23m. 

3  5°o    435 

4246 

7 

IO.OO  A.M. 

239 

25.0 

IOI 

5.0      3h.  38m. 

5  680    997 

[layer  at  12.24  P.M. 

4253 

7 

1.  00    P.M. 

239 

24-5 

99 

7.6      7h.  3&m. 

IO02O     341 

Agitsted    surface  of    sand 

4257 

7 

2.43       " 

239 

25.0 

IOI 

2.0      Sh.  17111. 

12  870 

336 

Agitated    surface  of    sand 

4258 

"       7 

4-59      " 

240 

23-5 

95 

3.3      ih.  34m. 

2  364 

247 

layer  at  2.  12  P.M. 

4275 

"       8 

5.10     " 

241 

23.5 

95 

2.9 

54'n. 

I  360 

99 

4280 

9 

10.25  A.M. 

242 

24.0 

97 

2.1 

22m. 

522        Ij 

4283 

9 

12.  2O    I'.M. 

242 

23.0 

93 

4-7 

2h.  I7m. 

3  192        o 

4302 

9 

3.25       " 

242 

25.0 

IOI 

6.3      sh.  2om. 

7  562      14 

Agitated  surface  of  sand  layer 

4315 
4318 

'        IO 
"        10 

11.15  A.M. 
I.Og   P.M. 

243 
243 

25.0 
21.5 

IOI 

87 

4.9      2h.  um 
9.6      4h.  O5m. 

4  292      38 

5  982      50 

at  2.15  C.M.  and  4.35  P.M. 
Agitated  'surface    of   sand 

4321 

"        IO 

3-M       " 

=44 

25.0 

101 

2-3 

5Om. 

i  281       29 

layer  at  1.27  P.M. 

4325 

"       10 

5.29       " 

245 

25.0 

IOI 

2.0 

22111. 

534      44 

4329 

"     II 

10.37  A.M. 

245 

24-5 

99 

4-1 

2h.  oom. 

2  934;     39 

4334 

"     II 

1.  08    I'.M. 

246 

25.0 

IOI 

2.  I 

3Sm. 

920        3 

4347 

"     II 

3-14       " 

247 

23-5 

95 

1-9 

17111. 

394        3 

4362 

"     II 

5.08       " 

247 

19-5 

79 

2h.  um. 

3°44      52 

4369 

"    13 

10.30  A.M. 

248 

25.0 

IOI 

1.9 

13111. 

363       22 

437" 

'    13 

11.51       " 

248       24.5 

99 

3.6      ih.  34tn. 

2  383        25 

4373 

'    13 

3.00   I'  M. 

248     !25.o    101 

5.1      4h.  43m. 

6973 

73 

4378 

'    13 

5-'5       " 

249     25.0 

IOI 

1.71            04m. 

I  80 

58 

4397 

'    14 

10.21   A.M. 

249    25.0 

IOI 

4.2       ih.  4om. 

2  040        5 

[layer  at  12.16  P.M. 

4410 

'     M 

1.27    P.M. 

249     25.0 

IOI 

5-1 

4h.  44111. 

7020        7 

Agitated   surface   of   sand 

4423 

'     14 

3.29       " 

249      25.0    ioi 

5.8 

6h.  44111 

99'°i       9 

Agitated    surface   of   sand 

4426 

'      14 

5-21        " 

250 

25.0    ioi 

1.9 

14111. 

423 

2 

layer  at  3.21  P.M. 

4430 

"      '5 

10.31    A.M. 

250 

25.01   ioi 

2.8 

Ih.  55m. 

4203 

6 

443' 

'      15 

11.32       " 

250 

25.0    ioi 

2.8 

2h.  55m. 

4  228 

23 

Agitated  surface   of    sand 

4432 

'      15 

n-33     " 

250 

25.0    ioi 

2.8 

2h.  56111. 

4253 

5 

layer  at  11.28  A.M. 

4433 

'     15 

n-34     ' 

250 

25.0    ioi 

2.8 

2h.  57m. 

4278 

2 

4434 

'     15 

n.35     ' 

250 

25.0    ioi 

2.8 

2h.  58m. 

4293 

5 

1 

4435 

'     ID 

11.36     " 

250 

25-5 

103 

2.8 

2h.  5gm. 

4318 

4 

i 

443<> 

'      >5 

11.37     " 

250 

26.0 

105 

2.8 

3h.  oom. 

4348 

9 

i 

4437 

ID 

11.38     " 

250 

25.0 

IOI 

2.8 

3h.  oim. 

4373 

II 

I 

4438 

'     '5 

11.39     " 

250 

25.0 

IOI 

2.8 

3h.  02m. 

4398 

6 

4439 

"     15 

11.40     " 

250 

25.0 

IOI 

2.8 

3h.  03111. 

4423 

15 

4440 

'     15 

11.57     " 

250 

25.0 

IOI 

3.0 

3h.  2om. 

5833 

9 

4441 

'      '5 

12.58  P.M. 

250 

25-5 

103 

5.0 

4h.  21  in. 

6393 

3 

4444 

'      15 

2.  II       " 

250 

25.0 

101 

7-7 

5h.  34"i 

7233 

3 

4449 

'     '5 

3.26      " 

250 

26.0 

105 

6.8 

6h.  47111 

9973 

16 

Agitated    surface  of   sand 

4453 

"     ID 

5.2O      " 

251 

25.0 

101 

2.2 

27111 

706 

12 

layer  at  3.04  P.M. 

4457 

"     16 

9.42  A.M. 

251 

25.0 

IOI 

2.9 

ih.  mm 

i  846 

9 

4460 

"      15 

1  1.  06       " 

25' 

25.0 

IOI 

5-7 

2h.  43111 

3936 

8 

4470 

•'     16 

I.I4    P.M. 

251 

25.0 

IOI 

4.0 

4h.  44111 

6  906 

5 

Agitated    surface   of   sand 

4474 

"      16 

2.45       " 

251 

25.0 

IOI 

7-1 

6h.  ism 

9  '3<> 

3' 

layer  at  12.42  P.M. 

4496 

'•     16 

5.03       " 

252 

25.0 

IOI 

2.1 

29111 

582 

2 

4504 

"      17 

2.45     ' 

252 

25.0 

IOI 

3-5 

2h.  o6m 

3052 

5 

45"! 

"     18 

lO.lg  A.M. 

253 

25.0 

IOI 

2.O 

05111 

146 

32 

4512 

"     18 

IO.24       " 

253 

24-5 

99 

2.O 

lorn 

256 

'9 

4513 

"     18 

0.29       " 

253 

25.0 

IOI 

2.  I 

15111. 

386 

45M 

"      18 

0.34       ' 

253 

25.  c 

101 

2.2 

2om. 

5°f 

4515 

"     IS 

o-39     " 

253 

25.0 

IOI 

2-3 

25111. 

636 

12 

4516 

"     18 

0.44     " 

253 

25.0 

IOI 

2.4 

3om. 

766 

IO 

45'7 

"      18 

0.49     " 

253 

25.  c 

IOI 

2.4 

35"'- 

906 

5 

4518 

"     18 

0.54     " 

253 

25.  c 

IOI 

2-5 

4001. 

I  006 

8 

4519 

"     18 

0.59     " 

253 

2;  .  1 

IOI 

2-5 

15111 

I  136 

8 

1 68 


WATER  PURIFICATION  AT  LOUISVILLE. 

TABLE    No   4. — Continued. 
Jewell  System. 


Ra 

teof 

„• 

tj 

Collected. 

Fill 

ation. 

£ 

c 

J5 

^ 

w 

£ 

Period  of 

w  c" 

3 

u 

Number 

Q. 

c  u 

T3 

Service  Since 

ii£  *J 

u 

e 

of 
Run. 

OtJD 

X 

WaswU 

£|$ 

S.| 

Remarks. 

x 

Hours  and 

Date. 

Hour. 

O   C 

lu  = 

O 

Minutes. 

u  3)  '-5 

4>  C 

3 

!B  " 

ii  rt  3 

Ur1* 

X 

3*^ 

u 

sa" 

J 

£ 

03 

1896 

4520 

July    18 

.04  A.M. 

253 

25.0 

01 

2-7 

5om. 

1276 

5 

4521 

"       18 

.og      " 

253 

25.0 

OI 

2.8 

55m. 

1386 

235 

4522 

"       18 

.14      ' 

253 

25.0 

OI 

3-0 

ih.  oom. 

1  526 

83 

4523 

"       18 

.29     " 

253 

25.0 

01 

3-1 

ih.  ism. 

2  CK)6 

4526 

"       18 

•44      ' 

253 

25.0 

01 

4-1 

ih.  3om. 

2  286 

S 

4531 

"       18 

•59      " 

253 

25.0 

OI 

4-7 

ih.  45m. 

2  676 

5 

4532 

"       18 

.14  P.M. 

253 

25.0 

OI 

5-5 

2h.  oom. 

3056 

5 

4533 

"       18 

.44      " 

253 

25.0 

01 

7-4 

2h.  3om. 

3886 

8 

4534 

"       18 

.14      ' 

253 

23.0 

93 

9.1 

3h.  oom. 

4516 

4 

4535 

"       18 

.21       ' 

253 

24.0 

97 

3-5 

3h.  05111. 

4616 

4 

Agitated  surface  of  sand 

4536 

"       IS 

.22       " 

253 

23   5 

95 

3-5 

3h.  o6m. 

4  f'59 

97 

layer  at  1.19  P.M. 

4537 

"       18 

.23       " 

253 

15-0 

61 

3-5 

3h.  07m. 

4659 

182 

4538 

"       18 

.24       ' 

253 

18.0 

73 

3-6 

3h.  07m. 

4<>59 

62 

Wasting  I  min.,  2ocu.  ft. 

4539 

"       18 

•25       ' 

253 

18.0 

73 

3-6 

3h.  O7m. 

4659 

30 

"       2     "       40 

4540 

"       18 

.26       " 

253 

22.5 

3-7 

3h.  o~m, 

4659 

27 

"       3     "       65      " 

4541 

"       18 

.27       " 

253 

21-5 

87 

3-7 

3h.  0701. 

4659 

17 

Opening  outlet. 

4542 

"       18 

.28       " 

253 

22.5 

3-8 

3h.  o8m. 

4691 

12 

4543 

"       18 

.2g       " 

253 

23.0 

93 

3-8 

3h.  ogm. 

4721 

14 

4544 

"       18 

.30       " 

253 

23-5 

95 

3-8 

3h.  lorn. 

474f> 

6 

4545 

"       18 

•44     ' 

253 

25-5 

103 

4.6 

3h.  24m. 

5  196 

17 

4553 
4554 

"       18 
"       18 

.14     ' 
•44      ' 

253 
253 

25-5 
25.0 

103 

IOI 

6.6 

8.2 

3h.  54m. 
4h.  24m. 

5846 
6  596 

I 

[layer  at  3.19  P.M. 

4556 

"       18 

3-14      " 

253 

25.0 

IOI 

9-7 

4h.  54m. 

7286 

9 

Agitated  surface  of  sand 

4557 

18 

3.24           '' 

4h.  59m. 

7  296 

157 

Wasting  2  min.,  45  cu.  ft. 

4559 

"       18 

3-44     " 

253 
253 

25.0 

IOI 

7-7 

5h.  ism. 

7  776 

10 

4560 

"       18 

4.14     " 

253 

22.  0 

89 

9-3 

5h.  45m. 

8496 

.  42 

4565 

18 

5-21        ' 

254 

25.0 

IOI 

2.0 

2im. 

53° 

5 

4571 

"       20 

11.15  A.M. 

254 

25.0 

IOI 

5.0 

2h.  44m. 

4  160 

10 

4573 

"         20 

1.32  P.M. 

254 

25.0 

IOI 

4-1 

4n.  5gm. 

7430 

12 

Agitated  surface  of  sand 

4578 

"         20 

3-52       " 

255 

26.5 

107 

2.  I 

1  6m. 

421 

3 

layer  at  1.20  P.M. 

458o 

"         20 

5.09       " 

255 

25.0 

IOI 

3-6 

ih.  33m. 

2361 

II 

4606 

"         21 

I2.OO    M. 

256 

25-5 

103 

3-8 

47111. 

I  180 

18 

[layer  at  1.08  P.M. 

4609 

"         21 

I.  2  I    I'.M. 

256 

25.0 

IOI 

2-7 

2h.  osm. 

3070 

26 

Agitated  surface  of  sand 

4612 

"         21 

3.12       " 

256 

24.0 

97 

5-8 

3h.  56m. 

5850 

44 

[layer  at  4.36  P.M. 

4615 

21 

5.07       " 

256 

24.0 

97 

7-2 

5h.  4gm. 

8620 

IOI 

Agitated  surface  of  sand 

4620 

22 

Il.Og  A.M. 

257 

25.0 

IOI 

45m. 

I  495 

M3 

Shut  inlet  and  outlet  H.IOA.M. 

4622 

"         22 

11.59      " 

31  in. 

93° 

87 

Shut  outlet  11.59  A.M. 

4623 

"         22 

12.33    I'-M. 

259 

34-0 

138 

3-4 

I2I11. 

354 

32 

4625 

"         22 

2.18       " 

260 

22.  O 

89 

4.8 

54111. 

i  44i 

248 

Agitated  surface  of  sand 

4631 

"         22 

4-45     " 

26! 

25.0 

IOI 

2.8 

33m. 

858 

745 

layer  at  2.45  P.M. 

463!- 

''         23 

11.23  A.M. 

263 

21.0 

85 

3.0 

44111. 

979 

51 

4644 

!!    23 

1.02  P.M. 

263 

22.0 

89 

2.0 

2h.  2im. 

2969 

124 

Agitated  surface  of  sand 

4646 

3-45      " 

264 

2O.  O 

8  1 

2.1 

39111. 

877 

g6 

layer  at  12.16  P.M. 

4647 

"         23 

4-54     " 

264 

20.0 

81 

9-9 

2h.  i8m. 

2877 

141 

4<>79 

!         24 

1.03     " 

266 

20.0 

81 

6.0 

ih.  32m. 

I  737 

60 

4687 

'         24 

2.46     " 

266 

20.5 

83 

4-5 

3h.  I3m. 

3  537 

27 

Agitated  surface  of  sand 

4688 

24 

3.18      " 

266 

22.  O 

89 

8.0 

3h.  45m. 

4  197 

126 

layer  at  1.54  P.M. 

4693 

24 

5.02     " 

267 

20.5 

83  . 

1.8 

33111. 

657 

[layer  at  10.23  A.M. 

4706 

25 

11.14  A.M. 

267 

22.  O 

89 

3h.  I3in. 

3947 

52 

Agitated  surface  of  sand 

4709 

25 

1.07  P.M. 

268 

21-5 

87 

1.6 

I  2111. 

264 

40 

[layer  at  1.56  P.M. 

4713 

'         25 

3.21      " 

268 

20.5 

83 

5-4 

2h.   15m. 

2  824 

Agitated  surface  of  sand 

4718 

'         25 

5-03      " 

268 

21.  0 

85 

5-0 

3h.  4&m. 

4614 

70 

Agitated  surface  of  sand 

4724 

27 

9.OO  A.  M. 

268 

32 

layer  at  4.10  P.M. 

4728 

"         27 

11.48       " 

269 

20.5 

83 

2.2 

2h.  I7m. 

2778 

7 

Agitated  surfaceof  sand 

473' 

'         27 

2.  02    P.M. 

269 

?o.o 

81 

7-3 

4h.  3im. 

3424 

38 

layer  at  11.05  A.M. 

4735 

27 

3  .  1  6     " 

269 

21.0 

85 

4.1 

5h.  43in. 

7038 

M 

Agitated  surface  of  sand 

4737 

27 

5.02    " 

269 

21.0 

85 

8.7 

7h.  22m. 

9078 

12 

layer  at  2.47  P.M. 

4770 

"    28 

11.26  A.M. 

270 

25.0 

101 

2.3 

2  I  111  . 

525 

4 

4782 

"     28 

1.  06  P.M. 

270 

23-5 

95 

2.8 

ih.  58m. 

2  765 

8 

Agitated  surface  of  sand 

4810 

"     29 

9-37  A.M. 

271 

24.O 

97 

1-7 

04m. 

no 

9 

layer  at  12.46  P.M. 

4811 

1     29 

9.42       " 

271 

24.0 

97 

1.7 

ogm. 

250 

6 

4814 

29 

9-47     ' 

271 

24.0 

97 

I4m. 

350 

3 

4815 

"     29 

9-52     " 

271 

24.0 

97 

i.i 

igm. 

470 

17 

COMPOSITION  Of  OHIO   RIVER    WATER   AFTER   PURIFICATION. 


169 


TABLE    No.   4. — Continued. 


Jewell  System. 


Rate  of 

j 

s 

Collected. 

Filtration. 

£ 

c 

•jj 

ji 

Number 

R 

Is 

•c 

Period  of 
Service  Since 

si- 

3 

o  u. 

B 

Run. 

s  u  s^i 

I 

Washing.       £j£ 

v  2i 

s 

Remarks. 

1 

Date. 

Hour. 

fcl      g'*! 

Hours  and       TS-^  o 

•£ 

I's   ig.? 

8 

223 

"CJ 

1 

0        S 

•3 

£ 

ffi 

.     1896 

4816 

July   29 

9.57  A.M. 

271 

23-5      95 

2.0 

24m.1        sgo 

10 

4817 

"      29 

10.  02        " 

271 

23-5,     95 

2.1 

2901.         700 

4 

4820 

1      29 

10.07    •• 

271 

23-5      95 

2.2 

34m.        820 

3 

4821 

29 

10.12       " 

2/1 

23-5      95 

2.3 

3gm.;       930 

3 

4822 

1      29 

10.17       " 

271 

23  5      95 

2.6 

44m.      i  060 

6 

4823 

1      29 

IO.22      " 

271 

23-5      95 

2.8 

4gm.     i  1  60 

12 

4824 

'      29 

10.27      " 

271 

23-5      95 

3-1 

54m.      i  2go 

10 

4825 

1      29 

10.32      " 

271 

23-5      95 

3.5 

5gm.     i  400 

5 

4827 

29 

10.47      ' 

271 

24.0      97 

5.i 

ih.  14111.     i  760 

10 

4828 

29 

11.02      " 

271 

22.5      91 

7-o 

ih.  2gm.      2  120 

IO 

4832 

29 

1.  17      " 

271 

22.5 

91 

9.2 

ih.  4401.     2440 

4833 

27  I 

ih.  57111.      *?  i<v\ 

70 

4835 

29 
"      29 

1.47     " 

•/  * 

271 

23.0 

93 

2.3 

2h.  o6m. 

2970 

/  V 

layer  at  11.27  A.M. 

4836!          "       29 

2.02    P.M. 

271 

23-5 

95 

2.5 

2h.  2lm. 

2  310 

13 

4838 

29 

2.17       " 

271 

23.0 

93 

2.7 

2h.  36m. 

3680 

II 

4839 

29 

2.32       " 

271 

23.0 

93 

3.0 

2h.  5im. 

4040 

8 

4841 

29 

2.47       ' 

271 

24.0 

97 

3-5 

3h.  o6m. 

4370 

i 

4842 

29 

1.02       " 

271 

24.5 

99 

3-8 

3h.  2im. 

4730 

21 

4845 

'      29 

1.34       " 

271 

23.5 

95 

5-0 

3h.  53m. 

553" 

25 

4848 

29 

2.02       " 

271 

23  5 

95 

5-7 

4h.  2im. 

6  1  60 

IO 

4850 

29 

2.32       " 

271 

22.  5 

91 

6.8 

4h.  5im. 

6840 

10 

4853 

29 

3  02     " 

271 

23.0 

93 

8.1 

5h.  2im. 

7  520 

12 

4859 

:      29 

3-34       ' 

271 

22.  0 

89 

9-2 

5h.  53m. 

8  290 

7' 

Agitated  surface  of  sand 

4864 

1      29 

5-3'J       " 

272 

24.0 

97 

i-7 

I5IT1. 

343 

14 

layer  at  3.49  P.M. 

Western    Gravity   System. 

608 

1095 
Dec.   23 

11.37  A.M. 

i 

IO.O 

Gi     

ih.  o2m. 

547 

495 

610 

"       23 

12.27   l'-M- 

i 

10    0 

6  1 

ih.  52m. 

i  018 

544 

614 

'       23 

3.22       " 

i 

IO.O 

61 

4h.  47m. 

2698 

328 

622 

24 

9-55  A.M. 

2 

IO.O 

6  1 

13111. 

1  66 

910 

623 

24 

10.25       '' 

2 

IO.O 

6  1 

43m. 

475 

510 

625 

24 

12.34    P.M. 

2 

IO.O 

6  1 

2h.  5201. 

i  700 

220 

632 

24 

3-25       " 

2 

IO.O 

6  1 

5h.  43m. 

3  5°6 

168 

635 

"       26 

9-57  A.M. 

2 

IO.O 

Gi 

8h.  32m. 

5  281 

580 

643 

"       26 

12.21    P.M. 

2 

IO.O 

61 

loh.  56m. 

6812 

580 

648 

"       26 

4.12       " 

2 

IO.O 

61 

I4h.  47m. 

9193 

288 

653 

"       27 

10.35  A.M. 

2 

IO.O 

61 

I7h.  3om. 

10  822 

570 

657 

1       27 

12.53  P.M. 

2 

IO.O 

61 

igh.  48m. 

ii  857 

540 

662 

27 

3.I8      " 

2 

5.0 

30 

22h  .  I3m. 

12  582 

324 

667 

1       27 

4.  23     " 

3 

18.0 

no 

I5m. 

232 

592 

668 

"       27 

4-44     ' 

3 

18.0 

no 

31111. 

544 

480 

677 

"       28 

10.  II    A.M. 

3 

17.0 

103 

2h.  I2m. 

2  309 

873 

680 

"       28 

11.47       " 

3 

8.0 

49 

3h.  48111. 

3329 

708 

687 

"       28 

3.27    P.M. 

3 

3.0 

18 

7h.  2Srn. 

4245 

I  260 

694 

"       30 

11.17  A.M. 

4 

6.0 

36 

3h.  55m. 

2652 

332 

699 

'      3° 

1.52    P.M. 

5 

14.0 

85 

iGm. 

203 

726 

702 

"      3° 

4-3S      " 

5 

II.  0 

67 

3h.  O2m. 

2456 

528 

7°9 

1  *              T  I 

O    ^A   A    M 

o 

1  5  m  . 

172 

276 

713 

"       31 

vO4  '*••  "*• 

11.05    ' 

6 

23.0 

140 

ih.  26m. 

I   141 

224 

720 

'       31 

2.18    P.M. 

6 

6.0 

36 

4h.  2401. 

3  15' 

260 

1896 

726 

Jan.    2 

IO.O4  A.M. 

7 

9.0 

55 

15111. 

150 

2OO 

728 

"         2 

10.34       " 

7 

8.5 

52 

45m. 

425 

ig2 

734 

2 

11.36       " 

7 

II.  O 

67 

ih.  47m. 

i  050 

136 

736 

"         2 

;  1.51  P.M. 

8 

10.  C 

61 

1  5m. 

122 

392 

737 

"         2 

2.21       " 

8 

12.0 

73 

45111. 

4/2 

304 

746 

"       3 

9.51   A.M. 

9 

7-5 

46 

1  5m. 

93 

250 

751 

1       3 

10.41       ' 

9 

9.0 

55 

ih.  o5m. 

55' 

208 

757 

1       3 

2.O8    P.M. 

10 

8.0 

49 

13111. 

119        .)!< 

759 

1       3 

2.40       " 

10 

9-5       S« 

45m. 

429      412 

762 

'      4 

11.29  A.M. 

II 

1  )  ' 

55 

19111. 

165         95 

767 

1       4 

12.0.)    P.M. 

II 

9  o 

"5 

54m. 

437        25 

770 

4 

2    18       "                                     II 

8.5      52    ••• 

3h.  o8m.      I  587       122 

170 


WATER  PURIFICATION  AT  LOUISVILLE. 

TABLE  No.  4. — Continued. 
Western  Gravity  System. 


Rate  of 

— 

8 

Collected. 

Filtration. 

w 

c 

o 

fr. 

A 

Number 

t 

jjs. 

Period  of 

«j  ="  . 

O  ^ 

£ 

a 

Run. 

So; 

X 

Last 
Washing. 

PI 

s| 

Remarks. 

5 

Date. 

Hour. 

61 

1*1 

Hours  and 
Minutes. 

w  rt  3 

11 

& 

u 

sa" 

.4 

£ 

1° 

1896 

777 

Jan.  6 

12.10  P.M. 

12 

14.0 

85 

ih.  27m. 

I  103 

416 

78i 

6 

3-33   " 

12 

8.0 

49 

4h.  som. 

2297 

320 

784 

"   7 

12.18   " 

12 

9.0 

55 

gh.  25m. 

5  193 

98 

788 

7 

3-49  " 

13 

i  i  .0 

67 

I5m. 

172 

92 

792 

7 

4.19   " 

13 

II.  O 

67 

45111. 

552 

88 

797 

8 

12.09   " 

13 

IO.O 

61 

5h.  ism. 

3512 

134 

800 

8 

2-33   " 

13 

IO.O 

61 

7h.  39111. 

5  002 

128 

804 

"   8 

3-04  ' 

13 

IO.O 

61 

8h.  lorn. 

5  288 

190 

808 

"   9 

IO.O9  A.M. 

14 

IO.O 

61 

14111. 

123 

76 

813 

9 

10.39   " 

14 

ii.  5 

70 

44m. 

443 

52 

818 

9 

2.O3  P.M. 

I4 

8.5 

52 

4h.  o8m. 

2  593 

172 

823 

'  10 

11-45  A.M. 

15 

12.  0 

73 

3h.  I7m. 

2275 

97 

830 

"  10 

1.56  P.M. 

15 

12.  0 

73 

5h.  28m. 

3935 

120 

833 

"  ii 

IO-54  A.M. 

16 

12.5 

76 

2gm. 

419 

53 

837 

"  ii 

11.28   " 

16 

13.5 

82 

ih.  03111. 

849 

135 

8523 

'  14 

11.07   " 

17 

II.  O 

67 

I5m. 

154 

57 

853 

"  14 

n-37  " 

17 

II.  O 

67 

45m. 

33 

861 

'  M 

2.12  P.M. 

17 

12.0 

73 

3h.  2om. 

2  321 

94 

864 

'  14 

3.09   " 

17 

ii.  o!  67 

4h.  I7m. 

2954 

60 

873 

'  15 

10.47  A.M. 

17    14-0 

85 

7h.  55m. 

5  554 

130. 

877 

'  15 

12.52  P.M. 

17 

13-0 

79 

i  oh.  oom. 

7  222 

go 

883 

"  15 

3-14   " 

17 

8.0 

49 

I2h.  22m. 

8793 

164 

889 

"  16 

10.58  A.M. 

18 

14.0 

85 

lorn. 

89 

48 

894 

"   16 

I.  Og  P.M. 

18 

20.  o 

122 

2h.  2om. 

2679 

ig2 

901 

"  16 

3.08   " 

18 

18.0 

no 

4h.  2om. 

4979 

150 

904 

"  17 

9-59  A.M. 

19 

15.0 

91 

o6m. 

70 

176 

9°5 

'  17 

10.03   ' 

19 

15.0 

91 

lorn. 

130 

124 

906 

"   17 

IO.I3   " 

19 

24.0 

146 

2om. 

320 

132 

907 

'  17 

10.23   " 

19 

25.0 

152 

3om. 

550 

141 

908 

'  17 

10.33   " 

19 

25.0 

152 

4Om. 

520 

102 

909 

'  17 

10.43   " 

19 

25.0 

152 

5om. 

i  080 

I32 

910 

'  17 

10.53   " 

19 

25.0 

152 

ih.  oom. 

i  376 

102 

926 

"  17 

I.  II  P.M. 

19 

2O.  0 

122 

3h.  iSm.i  4  500 

240 

929 

'  17 

2.04   ' 

19 

19.0 

116 

4h.  Iim.   5  500 

140 

933 

'  17 

3-°4   " 

19 

18.0 

no 

5h.  nm. 

6630 

238 

937 

"  17 

4.04   " 

19 

16.0 

97 

6h.  nm. 

7620 

188 

943 

"  J7 

5-08   " 

19 

7-5 

46 

7h.  ism. 

8380 

198 

946 

"  18 

9.56  A.M. 

20 

25.0 

152 

17111. 

460 

144 

951 

"  18 

IO.2O   " 

20 

26.0 

158 

41111. 

940 

258 

954 

"  18 

1.23  P.M. 

20 

27.0 

164 

3h.  44m. 

5  860 

256 

959 

"  18 

2.41   " 

20 

24.0 

146 

5h.  O2m. 

7869 

256 

967 

"   20 

IO.34  A.M. 

21 

22.  0 

134 

i6m. 

276 

192 

975 

"   2O 

4.25  P.M. 

21 

21.0 

128 

6h.  o7m. 

8  226 

246 

981 

"   21 

11.42  A.M. 

22 

25.0 

152 

2h.  osm. 

3  007 

M7 

987 

"   21 

4.25  P.M. 

22 

16.0 

97 

6h.  48m. 

8857 

202 

994 

"   22 

9-35  A.M. 

23 

25.0 

152 

I5m. 

265 

136 

995 

"   22 

10.05   ' 

23 

27.0 

164 

45m. 

i  155 

174 

999 

"   22 

2  28  P.M. 

23 

25.0 

152 

5h.  oSm. 

7955 

266 

1003 

"   23 

IO.I6  A.M. 

24 

28.0 

170 

5om. 

1345 

73 

1007 

"   23 

3-43  P.M. 

24 

21.  O 

128 

6h.  I7m. 

9655 

64 

1012 

"   24 

IO.08  A.M. 

25 

25.O 

152 

igm. 

409 

49 

1017 

"   24 

2.OO  P.M. 

25 

25.0 

152 

4h.  nm. 

6  &4g 

145 

IO2O 

"  25 

9.41  A.M. 

26 

28.5 

173 

I5m. 

397 

75 

1023 

"  25 

10.07   " 

26 

25.0 

152 

ih.  oim. 

2467 

65 

1027 

"  25 

2.23  P.M. 

26 

20.  O 

122 

4h.  57m. 

6509 

165 

1031 

"  27 

9.44  A.M. 

27 

23.0 

I4O 

I5m. 

322'  612 

1035 

"   27 

10.14   ' 

27 

23.O 

140 

45m. 

i  102   554 

1041 

"  27 

I.I3  P.M. 

27 

13-0 

79 

3h.  44m. 

4112   934 

1046 

"  27 

4.25   " 

28 

21.0 

128 

34m. 

689   504 

1055 

"  28 

1.  08   ' 

29 

I4.O 

85 

5om. 

I  015'  i  586 

1085 

"  31 

11.00  A.M. 

30 

2O.  0 

122 

5om. 

870'  278 

1088 

"  31 

2.33  P.M. 

31 

13.0 

79 

ih.  o6m. 

I  IOI    82O 

1097 

Feb.  i 

I2.I8   " 

32 

g.O 

55 

2h.  i8m. 

i  644!  326 

COMPOSITION   OF  OHIO   RIVER    WATER   AFTER  PURIFICATION. 


TABLE  No.  4. — Continued. 

Western   Gravity   System. 


Rate  of 

S 

0 

Collected. 

Filtration. 

u. 

Ji 

•j; 

i 

Number 

g. 

5  o- 

•a 

ServiceSince 

V   C* 

U  ^ 

i 

of 

« 

15  u  "• 

V 

Last 

>  ~  f 

n.  oj 

Remarks. 

^3 

Run. 

v  J 

O  u  - 

E 

Washing. 

!»^6S, 

g 

Date. 

Hour. 

fc.  5 

|J| 

0 

Hours  and 
Minutes. 

SS3 

'P 

•P 

IS 

rr  a  * 

n 

•—  —  U 

rt  ^ 

t/> 

u 

S        |    .2 

£ 

CO 

1896 

IIOO 

Feb.     I 

2.45  P.M. 

33 

18.0 

no 

4001. 

621 

137 

IIO.| 

I 

5.03      " 

33 

7.0 

43 

2h.  58111. 

2  8ll 

118 

no£ 

"       3 

IO.35  A.M. 

34 

17.0 

103 

3im. 

442 

240 

mi 

3 

I.l6   P.M. 

34 

12.  0 

73 

3h.  I2in. 

3  132 

632 

1113 

3 

3-23       " 

34 

22.  0 

134 

5h.  igm 

5  362 

560 

"7 

3 

5.00     " 

34 

6.0 

36 

6h.  56m. 

6742 

i  124 

122 

4 

10.22  A.M. 

35 

26.O 

158 

32m. 

780  1     421 

125 

4 

11.49      " 

35 

ig.O 

116 

ih.  5gm. 

2  SlO 

720 

128 

4 

2.31    P.M. 

35 

3-5 

21 

4h.  4im. 

4430 

908 

132 

4 

5.18      " 

36 

12.  O 

73 

ih.  5im. 

I  926 

900 

I38 

5 

IO.26  A.M. 

36 

I4.O 

85 

3h.  29111. 

3466 

600 

142 

5 

11.53       " 

36 

4.0 

25 

4h.  56m. 

4  168 

960 

146 

5 

3.14    P.M. 

37 

6.0 

36 

2h.  49111. 

2732 

324 

'51 

5 

5.09       " 

38 

15-5 

94 

41111. 

604 

308 

'57 

"       6 

IO.  22  A.M. 

38 

16.0 

97 

2h.  24111. 

2544 

,2. 

162 

"       6 

12.24   P.M. 

39 

20.  o 

122 

04111. 

58 

I  276 

165 

"       6 

3.I8      " 

39 

12.  O 

73 

2h.  5801. 

3  146 

655 

170 

"       6 

4.19      " 

39 

8.0 

49 

3h.  5gm. 

3718 

460 

'75 

"       7 

10.22  A.M. 

40 

18.0 

IIO 

5gm. 

i  252 

800 

179 

7 

1.37    P.M. 

41 

17.0 

103 

ih.  I2m. 

1639 

I  600 

1  88 

"       8 

10.37  A.M. 

42 

7.0 

43 

3h.  i6m. 

2  061 

321 

193 

8 

2.27    P.M. 

44 

16.0 

97 

32m. 

641 

825 

199 

8 

4-53     " 

45 

4.0 

25 

ih.  05111. 

403 

860 

206 

"       10 

10.35  A-M. 

46 

20.0 

122 

05  m. 

82 

252 

209 

"       10 

1.58    P.M. 

47 

6.0 

36 

ih.  33m. 

I  266 

272 

213 

"        10 

3-24       " 

48 

20.0 

122 

26m. 

493 

2go 

218 

"        IO 

5.07       " 

48 

13-0 

79 

2h.  ogm.     i  573 

672 

223 

"     II 

IO.I8  A.M. 

49 

g.O 

55 

57m- 

926 

251 

226 

"     II 

12.57    P.M. 

5" 

g.O 

55 

ih.  4om. 

'  458 

461 

229 

"     1  1 

3-  "9     " 

5' 

8.0 

49 

5601. 

983 

298 

233 

"     II 

5.15     " 

52 

6.0 

2Sm. 

37S 

950 

238 

"       12 

10.26  A.M. 

52 

S.o      49 

2h.  ogm. 

i  118 

2=0  Shut  outlet  10.26  A.M. 

244 

"       12 

4-53  I'.M.. 

56 

10.5       64 

ih.  22111. 

i  197 

605 

250 

"      '3 

9.54  A.M. 

57 

19.0    116 

33m. 

632 

1  06 

253 

'     13 

12.30    P.M. 

58 

23.0    140 

2im. 

458 

235 

256 

'     13 

2.25      " 

58 

4.0 

25 

2h.  i6m. 

2  158 

1045 

259 

'     '3 

4.41       " 

59 

8.5 

52 

ih.  4im. 

I  g8l 

425 

267 

'     M 

10.30  A.M. 

60 

18.0    no 

ih.  05111. 

I  348 

209 

271 

'      M 

1.22    P.M. 

60 

7-o 

43 

3h.  57m. 

3M8 

37' 

275 

'      M 

3-3°       " 

61 

20.  o 

122 

45111- 

946 

372 

1279 

'      M 

4  52      " 

6  1 

6.0 

36 

2li.  07  m 

2  246 

408 

1285 

"      15 

10  20  A.M. 

62 

iS.o 

IIO 

ih.  oim. 

I   500 

390 

1289            '     15 

1.33    I'.M. 

63 

17.0    103 

o6m. 

104 

5>7 

'293 

'      '5 

3.13       " 

63 

16.0 

97 

ih    4&m. 

2  I34 

'  975 

1298 

'      15 

5.24       " 

63 

9.0 

55 

3h.  57tn 

3424 

919 

1308 

'     17 

1     17 

10.19  A.M. 
1.45    I'-M. 

64 
65 

22.  O 
23.0 

134 
140 

ih.  oom. 
30111. 

'  474 
609 

865 
650 

1312 

'      "7 

3-13       " 

65 

lt,.n 

97 

ih.  58111. 

2409 

732 

'3'3 

'     '7 

3.2S       " 

65 

'3-5 

B2 

2)1.  13111. 

2659 

I  097 

1316 

"     17 

5.'4       ' 

65 

6.0 

36 

3h.  59»i. 

3389 

602 

1322 

'      18 

IO.32  A.M. 

66 

20.5 

135 

ill.  06111. 

i  396 

i  220 

1326 

"      IS 

12  05    P  M. 

66 

7-0 

43 

2h.  39111. 

2  766 

8co 

1330 

"     18 

2.3O       " 

67 

22.0 

'34 

41  m. 

788 

4^5 

1335 

"     18 

5.OO       " 

67 

g.O 

55 

3(1.  urn. 

3068 

'33 

1338 

"     18 

5.08       " 

67 

7-» 

43 

3h.  19111. 

3  128 

616 

'345 

"     19 

10.24  A-M- 

68 

20.0 

122 

ih.  08111. 

i  308 

158 

'319 

'     19                       11.40     " 

68 

8-5 

52 

2h.  2401. 

2498 

221 

1353 

'     19                       3.11   r  M. 

69 

IS.  5 

113 

ih.  42111. 

2  3IO 

1305 

'355 

'     '9 

4-55       ' 

69 

5-o 

3° 

3h.  26m. 

3310 

184 

11      2" 

1  1.09  A.M. 

70 

27.0 

164 

15111. 

385 

118 

1373 

"       20 

I.I9    P.M. 

7" 

6.0 

36 

2h.  25111. 

2405 

240 

1379 

"       20 

3.22       " 

71 

25-0 

152 

36111. 

828 

435 

1383 

"      30 

5-05       " 

71 

-.M 

49 

2)1.  Igm 

2328!      371 

172 


WATER  PURIFICATION  AT  LOUISVILLE. 

TABLE  No.  4. — Continued. 
Western    Gravity    System. 


Ra 

tepf 

S 

0 

Collected. 

Fill 

fc 

il 

'£> 

^ 

»- 

f.  V- 

Period  of 

v.  ^ 

O 

Number 

a 

o  a 

£ 

3 

Last 

•s"i  v 

£  i 

Remarks. 

a 

Run. 

re 

Washing. 

7, 

Date. 

Hour. 

fc.  ^ 

§ul 

Hours  and 
M  inutes. 

1-3 

•c  = 

•£ 

|l 

S  c.  JT 

y. 

—  2(j 

"u 

& 

U 

s 

~ 

h 

(3 

1896 

1391 

Feb.  21 

10.03  A.M. 

72 

24.0 

146 

3001. 

613 

89 

1396 

"   21 

12.49  I'-M. 

72 

4.0 

25 

3h.  l6m. 

2  513 

49 

1399 

"   21 

3.12   " 

73 

14.0 

85 

ih.  42m. 

2085 

310 

1402 

"   21 

5.00  " 

73 

4.0 

25 

3h.  35m. 

2805 

308 

1419 

"   24 

10.  ig  A.M. 

74 

23.0 

140 

ih.  oim. 

I  310 

212 

1425 

'   24 

1.25  P.M. 

74 

4.0 

25 

4h.  o7m. 

4  170 

2f)2 

1428 

"   24 

3.30   " 

75 

15.0 

91 

ih.  49111. 

2  282 

2<.g 

1433 

"   24 

5.21   ' 

75 

4.0 

25 

3h.  4Om. 

3250 

2fo 

1439 

"   25 

10.35  A.M. 

76 

22.0 

'34 

ih.  1  6m. 

i  749 

I  495 

1443 

"   25 

I.  21  P.M. 

76 

g.o 

55 

4h.  O2m. 

5  1  19 

680 

1447 

"   25 

3.15   " 

77 

25.0 

152 

42m. 

949 

605 

1450 

"   25 

4-55   ' 

77 

5-o 

3" 

2h.  22m. 

2543 

I  270 

1458 

"   26 

IO.32  A.M. 

78 

20.  o 

122 

o6m. 

91 

475 

1462 

"   26 

12.15  r-M. 

78 

21.5 

131 

ih.  49m. 

2471 

480 

1466 

"   26 

3.12   " 

78 

15-0 

9T 

4h.  46m. 

5971 

700 

1468 

"   26 

5-  II   ' 

78 

2.O 

12 

6h.  45m. 

6801 

962 

1476 

"   27 

IO.3O  A.M. 

79 

25.  ( 

152 

ih.  2om. 

i  82g 

455 

1481 

"   27 

1.48  P.M. 

79 

6.0 

36 

4h.  38m. 

5  519 

630 

1485 

27 

3.  of) 

So 

27-5 

If)7 

48111. 

i  177 

337 

1490 

27 

5.15   " 

So 

8.0 

49 

2h.  57m. 

4037 

48,, 

1498 

"   28 

10.46  A.M. 

So 

12.  0 

73 

4h.  58m. 

5937 

129 

1503 

"   28 

3.26  P.M. 

Si 

24.0 

146 

3h.  I4m. 

4864 

445 

1505 

"   28 

4-57  " 

81 

14.  < 

85 

4h.  45m. 

6774 

485 

1515 

"   29 

10.40  A.M. 

81 

4.1 

25 

6h.  i6m. 

7524 

235 

1518 

29 

1.40  P.M. 

82 

25.0 

152 

2h.  4Sm. 

3880 

35" 

1522 

2g 

3-23   " 

82 

23.0 

140 

4h.  3im. 

6330 

905 

1525 

29 

5.05   ' 

82 

12.0 

73 

6h.  ism. 

8550 

i  115 

1534 

Mar.  2 

9.46  A.M. 

82 

24.' 

146 

7h.  24m. 

9  5oo 

357 

1538 

"     2 

IO.27   " 

82 

22.  0 

134 

8h.  0501. 

104015 

1542 

2 

1.39  P.M. 

S3 

27.1 

164 

2fmi  . 

620 

i  685 

1546 

2 

3.21   ' 

S3 

22.0 

134 

2h.  o8m. 

2  850 

4  ooo 

1551 

2 

5-13   " 

83 

15." 

g  I 

4h.  oom. 

5  380 

i  735 

1559 

"    3 

10.45  A.M. 

S3 

25.< 

152 

6h.  O2m. 

7  720 

i  280 

1563 

3 

12.55  I'.M. 

S3 

20.1 

122 

8h.  I2m. 

10659 

i  005 

. 

1572 

3 

5.16   " 

i6.( 

97 

ih.  57m. 

2  512 

goo 

1578 

4 

IO.5I  A.M. 

84 

23.0 

140 

4h.  O2m. 

5  202 

i  175 

1582 

4 

1.02  P.M. 

84 

23.  < 

140 

6h.  I3m. 

8  212 

610 

1586 

4 

3.23   " 

'   84 

20.  o 

122 

8h.  34m. 

II  122 

328 

1591 

4 

5.07   ' 

84 

7-0 

43 

loh.  iSm. 

12  892 

660 

1597 

5 

10.42  A.M. 

85 

19.0 

116 

37m. 

759 

795 

1601 

5 

12.57  I'.M. 

85 

23.5 

M3 

2h.  52m. 

3  7<>9 

i  085 

1606 

5 

3-24   " 

85 

23.0 

140 

5h.  igm. 

7  129 

745 

1610 

5 

5.  II   ' 

85 

17.0 

103 

7h.  o6m. 

9459 

5f>5 

1618 

"   6 

10.38  A.M. 

85 

19.0 

116 

gh.  O3m. 

"499 

39" 

1623 

6 

12.44  I'-M. 

85 

7.0 

43 

nh.  ogm. 

13449 

237 

1628 

6 

3.24   ' 

86 

25.0 

152 

2h.  1401. 

2909 

5<X) 

1631 

6 

5.19   " 

86 

23-0 

140 

4h.  ogm. 

5619 

245 

1639 

7 

10.50  A.M. 

86 

20.  o 

122 

6h.  lorn. 

8  159 

174 

1^45 

7 

3.14  P.M. 

87 

25.0 

152 

ih.  4im. 

2  256 

477 

1652 

7 

5-22   " 

87 

12.0 

73 

3h.  4gm. 

5  KJ& 

345 

1658 

7 

I  I.  Of)  A.M. 

87 

12.0 

73 

6h.  o^m. 

7456 

194 

1663 

9 

12.55  I'-M. 

88 

21.0 

128 

56m. 

i  204 

401 

1667 

9 

3-27  " 

88 

24.0 

146 

3h.  28m. 

4  f'34 

525 

1674 

9 

5.10  " 

88 

8.0 

49 

5h.  nm. 

6414 

5'5 

Id.So 

'   o 

IO.26  A.M. 

89 

22.5 

137 

ih.  O7rn. 

i  509 

26=; 

1684 

"   o 

I.3S  P.M. 

Sg 

23.0 

140 

4h.  igm. 

5  f'49 

168 

1689 

0 

3.12  " 

89 

19.  o 

116 

5h.  53m. 

7689 

157 

lG95 

"   o 

5.19   " 

Sy 

4.0 

25 

8h.  oom. 

9  179 

210 

1702 

"   i 

11.25  A.M. 

25-0 

152 

ih.  1401. 

i  f)2g 

1  86 

1704 

"   i 

1.33  I'.M. 

90 

23.0 

140 

3)1.  22m. 

4399 

141 

1708 

"   i 

3-25   " 

go 

20.0 

122 

5h.  I4m. 

6829 

234 

1715 

"   i 

5.  if-  " 

90 

8.0 

49 

7h.  o5m. 

8789 

161 

1721 

"    2 

IO.22  A.M. 

91 

23.0 

140 

ih.  0701. 

i  584 

250 

COMPOSITION  OF  OHIO   RIVER    WATER   AFTER   PURIFICATION. 


'73 


TABLE  No.  4. — Continued. 

Western    Gravity    System. 


Rate  of 

J 

0 

Collected. 

Filtration. 

i 

~ 

•5 

fc 

Number 

t 

c  a 

Period  of 
•c     Service  Since 

V.   tC 

u  u- 

1 

Run. 

t   . 

§££ 

£        Washing. 

•L.   <*   V 

&gu. 

if  " 

Remarks. 

f. 

Date. 

Hour. 

o! 

g<| 

Hours  and 
°         Minutes. 

~| 

•'z 

II 

S  a  ? 

"                                -2,3(3 

"CJ 

y> 

U 

s 

2                             •  £ 

00 

1896 

1725 

Mar.  12 

1.  00  P.M. 

9' 

24.0 

146 

....       3h.  45m.  i    5  114 

140 

173° 

"        12 

3-31       " 

91 

20.0 

122 

....       6h.  i6m.      8  404 

146 

1735 

"       12 

5-17      ' 

91 

5-0 

30 

....       8h.  O2m.|  10014 

112 

1741 

"     13 

IO.29  A.M. 

92 

23-5 

143 

....       ih.  O7m.i    i  479 

440 

1745 

'     13 

I.I5    P.M. 

92 

22-5 

137 

3h.  53m.      5  317 

213 

1749 

'     13 

3.19       " 

92 

19.0 

116 

5U.  57m.      7  927 

I2g 

1754 

'     13 

5-04       ' 

92 

8.0 

49 

7h.  42m.     9  507 

152 

1761 

'      14 

10.36  A.M. 

93 

23.0 

140 

....       ih.  24111.      i  926 

127 

1767 

'     14 

I.  1  1    P.M. 

93 

22.  O 

134 

....      3h.  5gm. 

5  426 

128 

1773 

'      M 

3.16        " 

93 

16.0 

97 

....       6h.  04111. 

7856 

149 

1780 

'      14 

4-54        " 

93 

6.0 

36 

....       7h.  42m. 

9056 

158 

1787 

"     16 

10.33  A.M. 

94 

22.  0 

134 

....       ih.  1401. 

I  736 

131 

1793 

"      16 

I.O7  P.M. 

94 

20.  0 

122 

3h.  58m. 

5326 

490 

1799 

"     16 

3.20       " 

94 

4.0 

25 

....      6h.  oim. 

7og6 

2OO 

1805 

"     16 

5.07       ' 

95 

22.0 

134 

....      ih.  2om. 

i  824      187 

1813 

"      17 

IO.32  A.M. 

95 

20.0 

122 

3h.  ism. 

4354      228 

1819 

'      17 

I.I7   I'.M. 

96 

24.0 

146 

4om. 

953      157 

1825 

'      17 

3-23       " 

96 

22-5 

137 

2h.  46111. 

3  803      445 

1829 

'     17 

5.09       " 

96 

8.0 

49 

4(1.  32m. 

5  673      380 

1837 

'      18 

1O.32  A.M. 

97 

22.0 

134 

ih.  igm. 

i  879      730 

1843 

"      18 

I.  1  6    I'.M. 

97 

II  .O 

67 

4h.  03111. 

5  269      230 

1850 

"     18 

3-27       " 

98 

23.0 

140 

ih.  03111. 

1414      585 

1856 

"      18 

5.05       ' 

98 

22.0 

134 

2h.  4101. 

3  544      535 

1864 

"      19 

I0.5O  A.M. 

99 

ig.o 

116 

I2m. 

179 

440 

1872 

'     19 

1.22    P.M. 

00 

21.0 

128 

1  5m. 

265 

800 

1876 

'     19 

3.05       " 

00 

6.0 

36 

ih.  58m. 

1  985      580 

1890 

'       20 

IO.3O  A.M. 

01 

24.0 

146 

2im. 

468  i  ooo 

1896 

"       20 

I.  12    P.M. 

03 

1.0 

6 

5im. 

659 

7OO 

1898 

"       20 

I.46       " 

04 

20.0 

122 

o6m. 

137 

500 

4145 

July     2 

10.32  A.M. 

07 

14.5 

88 

55m. 

756      130 

4146 

2                               11.14 

"7 

ih.  37m. 

1239:       68  Shut  outlet  11.14  A.M. 

4154 

"          2                                  2.24   I'.M. 

09 

i  h    iGm 

i  029!  i  500  A.  Shut  outlet  2.24  P.M. 

4158 

2                                  3.07       " 

10 

14.0 

85 

i8m. 

225        52 

4166 

3                               IO.I8  A.M. 

12 

14.0 

85 

3  8 

ih.  O2m. 

8gg;         g 

4178 

"          3                                  I.  1  2    P.M.                                  12 

3  h  .  56m. 

3  253        10  Shut  outlet  1.14  P.M. 

4187 

3                         1.56     "                           13 

15.0 

91 

nm. 

166        50 

4195 

3                         3.42     " 

14 

15.0 

9' 

3-o 

lorn. 

142        77 

4199 

3                         5-00     " 

M 

14.0 

85 

7.8 

ih.  28m. 

i  142 

62 

4316 

'         O                            11.22  A.M. 

15 

15.0 

91 

ih.  5om. 

I  682 

46 

4319 

0                                 1.22    P.M. 

15 

20.  o 

122 

3-5 

3h.  som. 

3632 

131 

4322 

"       o                       3.18     " 

15 

15-0 

91 

6.8 

5h.  46m. 

5242 

152 

4330 

"         I                             IO.47  A.M. 

16 

13-5 

82 

3-3 

ih.  32m. 

M37 

118 

(335 

'         I 

I.I5    P.M. 

1  6 

16.0 

97 

4-4 

4(1.  oom. 

3739 

199 

* 

4338 

"         I 

2.35      " 

16 

12.  0 

73 

2.  I 

o 

o 

5  ooo  Wast.  3  min.,    52  cu.  ft. 

4339 

"         I 

2.40    " 

16 

14.5 

88 

2.1 

o 

o       3000      "      7     "      112 

434" 

"         I 

2.45     ' 

16 

14.5 

88        2.2 

o 

0          I  300        "      12       "         182 

4341 

"         I 

2.50     " 

16 

14.5 

88        2.2 

0 

o          364      "     17     "      252 

4342 

I                         2.55     ' 

16 

14.5 

82 

2.2 

o 

O              392         "      22       "        312 

4343 

'        i                         3.00     " 

17 

18.0 

no 

I  .  I 

oom. 

o!     387  Opened  outlet  3.00  P.M. 

4344 

i                         3.05      " 

17 

15-5 

94 

1-5 

05111. 

5^1     234 

4345 

i 

3.10     " 

'7 

15-5 

94      i-5 

1  0111. 

146      213 

4348 

"        i 

3.15     ' 

17 

16.0 

97      2-5 

1  5m. 

236      204 

4349 

"        i 

3.20     " 

17 

'5-5 

94      2.5 

2om. 

326      157 

4350 

"        i 

3.25     " 

17 

'5-5 

94 

2-5 

25111. 

3g6      142 

4351 

"        i 

3.30     " 

17 

16.0 

97 

2.6 

3001. 

476      169 

4352 

i 

3-35     ' 

17 

II,  .0 

97 

2.6 

35m. 

54<>,     235 

4353 

"        i 

3-4"     " 

17 

16.0 

97 

2.6 

4om. 

616 

216 

4354 

"        i 

3-45      ' 

J7 

16.0 

97 

2-7 

45m. 

6g6 

199 

4355 

"        i 

3.50     " 

17 

16.0 

97 

2-7 

50111. 

776 

229 

435<> 

i 

3-55     ' 

17 

H,.,, 

97 

2-7 

55m. 

S5(, 

207 

4357 

"        i 

4.00     " 

17 

16.0 

97 

2.7 

ih.  oom. 

936 

4358 

"        i 

4."5      ' 

17 

16.0 

97 

3-2 

ih.  15111. 

I  176 

186 

435Sa 

"       I 

4-3"     " 

i- 

ii,.  ,, 

97 

3.6 

ih.  3001. 

1     )!'' 

271 

Wasting. 


174 


WATER   PURIFICATION  AT  LOUISVILLE. 
TABLE  No.  4. — Continued. 

Western    Gravity    System. 


Rate  of           ~ 

V 

Collected. 

Filtration. 

aj 

c 

.H       i 

u- 



fc, 

Period  of 

5i  ti 

JS 

3 

s 

Number 
Run. 

S. 

I8-  . 

-d 

DC 

Last 
Washing. 
Hours  and 

&£fc 

CJ     . 

«  E 

Remarks. 

Date. 

Hour. 

0  G 

its 

° 

Minutes. 

III 

I! 

u 

~  d  5 

1 

gj° 

m 

1896 

4359 

July    II 

4-45  P-M. 

117       15.5 

94 

3-9 

ih.  45m. 

1646 

4360 

"       II 

5-OO     " 

117       15.0      gi 

4.0 

2h.  oom. 

I  876 

4361 

"       II 

5.05     " 

117 

2h    o^m 

I  953 

176 

4505 

"       17 

2.52     " 

118 

15.0    91 

4-1 

54m. 

861 

33 

4524 

"       18 

11.34  A.M. 

118 

16.0      97 

6h.  o6m. 

5  723 

46 

4547 

"       IS 

1.57  P.M. 

ng 

16  .  o      97 

2-5 

22m. 

340 

36 

4555 

"       18 

3-12      " 

Ijg       16.0      97 

ih.  37m. 

I  540 

61 

4660 

'      24 

0.50  A.M. 

1  20      IO.O      6  1 

2.  I 

o 

o 

320  Wasting  33  min.,  334  cu.  ft. 

4661 

'      24 

I.OO      " 

121       16.0      g? 

2.5 

osm. 

61 

158 

4662 

'      24 

I.O5      " 

121       15.0      91 

2.6 

lorn. 

141 

168 

4663 

1       24 

I.IO      " 

121       15.0      91 

2.6 

I5m. 

211 

4664 

'       24 

I.I5      " 

121       15.0      91 

2.6 

2om. 

28l 

315 

4665 

'      24 

1.  2O      " 

121 

13-0      79 

2.1 

25111. 

351 

63 

4666 

'       24 

1.25      " 

121 

13-0      79 

2.2 

3Om. 

421 

268 

4667 

1       24 

1.30      " 

121 

13-0      79 

2.1 

35m. 

49! 

4668 

'       24 

1-35     " 

121 

'3-0      79 

2.2 

40m. 

561 

161 

4669 

'      24 

1.40    " 

121 

14.0      85 

2.5 

45m. 

611 

352 

4670 

'       24 

1.45     " 

121 

14-0      85 

2.4 

5om. 

691 

202 

4671 

'      24 

1.50     " 

121 

14-0      85 

2.4 

55m. 

751 

446 

4673 

'       24 

1.55     " 

121 

I4.o      85 

2.5 

ih.  oom. 

821 

157 

4674 

1       24 

2.IO  P.M. 

121 

14.0 

85 

2.6 

ih.  1501. 

I  051 

214 

4675 

'      24 

2.25      " 

121 

14.0      85 

2.6 

ih.  3Om. 

I  261 

165 

4676 

'      24 

2.40      " 

121 

14.0      85 

2.6 

ill.  45m. 

I  481 

178 

4677 

'      24 

2-55     " 

121 

14.0      85 

2.9 

2h.  oom. 

I  711 

112 

4680 

'      24 

I.IO      " 

121 

14.5      88 

2.9 

2h.  I5m. 

I  gu 

275 

4681 

1       24 

1.25   " 

121 

15.0      gi 

2-9 

2h.  3om. 

2  III 

177 

4683 

24 

1.40   " 

121 

15.0      gi 

3-0 

2h.  45m. 

2  321 

237 

4684 

'       24 

1-55     " 

121 

15.0      gi 

3h.  oom. 

2  541 

299 

4686 

'       24 

2.  IO      " 

121 

15.0      91 

3-1 

3(1.  15111. 

2  761 

498 

4702 

1       25 

IO.  IO  A.M. 

122 

12.  o      73 

o 

O 

Wasting  70  min.,  763  cu.  ft. 

4703 

'      25 

10.38      " 

122 

13.5      82 

23111. 

",OO 

'"So 

4707 

1       25 

I  I.2g      " 

122 

13.0      79 

6.7 

ih.  14111. 

980 

3041 

4708 

"       25 

1.  01       " 

122 

13.0      79 

7-2 

2h.  46111. 

2  I3O 

240 

4714           "       25 

4.38       " 

123 

12.5      76 

2.8 

48111. 

5'4 

511 

4883 

'      3' 

11.20      " 

124        14.0        85 

3-5 

2h.  15111. 

I  889 

450 

4888 

31 

2.O4  P.M. 

124        14.0        85 

5.1 

4h.  sgm. 

43'9 

104 

4889           "       31 

2.07      " 

124 

14.0      85 

6.0 

5h.  O2m. 

5189 

1  66 

4892             '       31                          3.38     "                           124 

13.5      82 

5-7 

6h.  33m. 

5639 

136 

Western  Pressure  System. 

1895 

607 

Dec.    23 

11.33  A.M. 

18.0    128 

58111.      I  070 

171 

609 

"      23 

12.24  P-M. 

20.0          142       ':.... 

ill.  4gm. 

1934 

260 

623 

23 

3.19      •' 

24.0    170 

4h.  4401. 

55SO 

172 

621 

24 

9.50  A.M. 

22.  0      156 

7)1.  1301. 

9  3'8 

295 

624 

24 

12.31    P.M. 

21.  0     149 

gh.  5401. 

I  2  960 

So 

631 

!       24 

3-22      " 

21.  OJ     149 

I2h.  45111. 

16568 

90 

f>34 

26 

g.5I  A.M. 

20.  o    142 

15)1.  26m. 

1  9  839 

860 

642 

"       26 

12.  17  P.M. 

17.0 

1  20 

17)1.  52111. 

22  596 

130 

647 

"         26 

4.09      " 

28.O 

199 

2ih.  44m. 

28  571 

242 

654 

"    27 

10.42  A.M. 

28.0 

199 

24h.  37m. 

33  239 

360 

656 

'     27 

12.5O  P.M. 

28.0 

199 

26h.  45m. 

36582 

480 

663 

'      27 

3-25     " 

22.0 

156 

2gh.  2Om. 

40  150 

268 

669 

"     27 

4-47     " 

2O.  O 

142 

30)1.  42111. 

41  631 

324 

676 

"    28 

lO.Og  A.M. 

19.5 

138 

31)1.  56m. 

43  336 

494 

678 

"     28 

11.15      " 

25.0 

177 

19111. 

588 

810 

679 

"        28 

11.45      " 

28.0 

199 

49111. 

I  460 

I  170 

686 

"        28 

3.25   P.M. 

22.0 

156 

4)1.  29111. 

6384 

I  1  16 

695 

"    30 

11.22  A.M. 

3 

20.  0 

142 

55m. 

984 

246 

700 

1     30 

1.55  P.M. 

3 

21.  0 

149 

3)1.  2801. 

4  280 

460 

703 

'    30 

4.43      " 

3 

23.0 

163 

6h.  16111. 

8067 

520 

710 

1     31 

IO.O5  A.M. 

4 

21.0 

149 

15m. 

303 

380 

714 

'       3t 

II.  10     " 

4 

23.5 

1  66 

ill.  2om. 

2  705 

143 

72i 

'       3' 

2.  2O  P.M. 

4 

22.5 

1  60 

4h.  3om. 

5  228 

280 

COMPOSITION  OF  OHIO   RIVER    WATER  AFTER   PURIFICATION. 


'75 


TABLE  No.  4. — Continued. 

Western    Pressure    System. 


Ra 

r  of 

w 

•J 

Collected. 

Filtr 

uion. 

tb 

•jj 

5 

. 

i. 

/  _ 

Period  of 

U  5? 

3 

1 

Number 

8. 

0  0. 

•o 

Service  Since 

«'^  t 

^  b 

a 

of 
Run. 

Soi 

5  si 

X 

\VasWng. 

£j£ 

aS 

Remarks. 

z 

Date. 

Hour. 

ul 

§<S 

•3 

Hours  and 
Minutes. 

T3-*  O 

•^•3 

| 

11 

i  !.? 

s 

J.35 

i" 

JS 

U 

s 

-> 

£ 

OS 

1896 

727 

Jan.  2 

IO.I8  A.M. 

5 

15-5 

IIO 

I5m. 

192 

236 

729 

"   2 

10.48   " 

5 

15-5 

1  10 

45m. 

672 

121 

735 

"   2 

"•39  " 

5 

19-5 

138 

ih.  36111. 

i  632 

I3O 

738 

"   2 

2.28  P.M. 

5 

16.0 

113 

4h.  25m. 

4752 

546 

m 

747 

3 

10.04  A.M. 

6 

21.  O 

149 

I5m. 

216 

1  60 

752 

3 

10.46   " 

6 

20.  0 

142 

57m. 

I  046 

140 

758 

3 

2.13  P.M. 

6 

18.0 

128 

4h.  24m. 

4876 

208 

763 

4 

II.3O  A.M. 

7 

12.0 

85 

I5m. 

194 

65 

768 

4 

12.07  P.M. 

7 

16.0 

113 

52m. 

721 

116 

769 

4 

2.15   " 

7 

14-5 

102 

3h.  oom. 

2  671 

120 

778 

6 

12.14   " 

7 

14.0 

99 

gh.  5im. 

8671 

1  86 

782 

"   6 

3.36   " 

7 

16.0 

"3 

I3h.  I3m. 

II  812 

228 

787 

7 

3-35   ' 

8 

20.  o 

142 

I5m. 

349 

82 

791 

"   7 

4-05   ' 

8 

20.  o 

142 

45m. 

936 

76 

796 

"   8 

12.05   ' 

8 

20.  0 

142 

5h.  25m. 

6860 

210 

80  1 

"   8 

2.36   " 

8 

18.0 

128 

7h.  56m. 

8584 

188 

805 

8 

3.10   " 

8 

18.0 

128 

Sh.  3om. 

9  I7<J 

314 

807 

9 

IO.O5  A.M. 

9 

17.0 

120 

2im. 

312 

73 

812 

9 

10.35   " 

9 

21.0 

149 

5im. 

go2 

22 

819 

9 

2.O6  P.M. 

9 

2O.  O 

142 

4h.  22m. 

5  152 

140 

824 

'   IO 

11.48  A.M. 

o 

loh  .  ogm. 

1  1  692 

118 

831 

"   IO 

2.00  P.M. 

9 

18.5 

132 

I2h.  iim. 

14  152 

184 

834 

"  II 

10.56  A.M. 

10 

19-5 

138 

28m. 

-  457 

130 

838 

"  II 

11.32   " 

IO 

20.0 

142 

ih.  04m. 

I  137 

177 

852b 

'  14 

II.I8   " 

n 

22-5 

1  60 

I5m. 

283 

42 

854 

'  14 

11.48   " 

ii 

21.0 

149 

45m. 

88; 

148 

862 

'  14 

2.18  P.M. 

ii 

20.  0 

142 

3h.  ism. 

3578 

62 

865 

"  14 

3.12   " 

ii 

19.  o 

"35 

4h.  ogm. 

4582 

IOO 

874 

"  15 

10.49  A.M. 

n 

22.  0 

156 

7h.  56m. 

9013 

136 

876 

'  15 

I2.5O  P.M. 

ii 

22.  0 

156 

gh.  57m. 

ii  732 

140 

884 

"  15 

3.20  " 

n 

24.0 

170 

I2h.  27m 

14973 

1  66 

890 

"  16 

11.02  A.M. 

ii 

21  .O 

149 

l6h.  o8m 

19993 

14 

895 

"   16 

I.I4  P.M. 

n 

29.O 

206 

i8h.  2om. 

23543 

104 

902 

"  16 

3.II  A.M. 

n 

27.0 

igi 

2oh.  I7m. 

26  92; 

248 

911 

"  17 

11.02   " 

12 

23.0 

163 

1501. 

375 

170 

914 

'  17 

11.32   " 

12 

28.0 

igg 

45m 

i  107 

927 

'  17 

I.l6  P.M. 

12 

27.0 

191 

2h.  2gm 

3827 

156 

928 

'  17 

2.  02   " 

12 

26.0 

184 

3h.  I5m. 

5067 

198 

934 

'  17 

3.17   " 

12 

28.0 

199 

4h.  3om 

7177 

236 

~"~ 

938 

'  17 

4.06   " 

12 

27.0 

191 

5h.  igm. 

8  597 

214 

944 

"  17 

5.13   " 

12 

25.0 

177 

6h.  26m. 

10  197 

34° 

95° 

"  18 

10.  16  A.M. 

12 

3O.O 

213 

7h.  2gm 

ii  897 

190 

955 

"  18 

1.28  P.M. 

12 

33-5 

224 

loh.  4im. 

'7997 

268 

958 

"  18 

2.39  " 

12 

30.0 

213 

iih.  52m. 

20347 

274 

966 

"  20 

IO.32  A.M. 

12 

23.0 

163 

I5h.  42m 

27057 

1  80 

970 

"   20 

1.53  I'.M. 

13 

27.0 

igi 

3om 

630 

212 

976 

"   20 

4.28  •' 

13 

29.0 

206 

3h.  o$m 

4960 

260 

980 

"   21 

11.37  A.M. 

'3 

28.0 

igg 

6h.  24111 

10340 

177 

988 

"   21 

4.30  P.M. 

13 

28.0 

199 

iih.  I7m 

18  700 

211 

993 

"   22 

9.29  A.M. 

'3 

24. 

170 

I2h.  i8m 

20600 

100 

ooo 

"   22 

2.33  P.M. 

13 

30. 

213 

I7h.  22m 

2g  780 

140 

004 

"   23 

10.19  A.M. 

13 

29. 

206 

2ih.  I4m 

36  250 

222 

006 

"   23 

3.40  P.M. 

13 

2O. 

142 

26h.  35m 

45  too 

130 

Oil 

"   24 

IO.O5  A.M. 

M 

25- 

177 

1701 

35i 

59 

016 

"   24 

1.55  I'-M. 

14 

30. 

213 

4h.  07m 

7ogi 

128 

02  1 

"  25 

9.52  A.M. 

14 

25- 

177 

8h.  03m 

14041 

103 

026 

"   25 

2.  2O  P.M. 

M 

24.0 

170 

I2h.  3im 

20  411 

170 

036 

"   27 

10.17  A.M. 

14 

26.0 

184 

I5h.  ogm 

24151 

635 

042 

"  27 

I.l6  P.M. 

M 

23.0 

163 

i8h.  o8m 

28531 

836 

047 

"  27 

4.3°   " 

15 

25.0 

177 

39m 

957 

770 

052 

"   28 

9.58  A.M. 

15 

26.0 

184 

2h.  04m 

3017 

1448 

056 

"  28 

3.20  P.M. 

15 

16.0 

"3 

6h.  4om 

8277 

736 

o6ia 

"   28 

4.40   " 

15 

14.0 

99 

Sh.  mi,,. 

')  l'>7 

444 

WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE   No.   4. — Continued. 

Western    Pressure    System. 


Rate  of          S 

g 

Collected. 

Filtration.       £ 

55  . 

'B 

s 

Number 

S. 

c  v 
_o  a        -a 

Period  of 
Service  Since 

>- 

U 

1 

Su 

•<      O                   VH| 

Last 
Washing. 

K 

d  V 

Remarks. 

•a 

Date. 

Hour. 

|.l 

Minutes. 

III 

V   - 

i 

O 

s&™    2 

E 

Jju 

1896 

06  1  b 

Tan    28 

4  080 

A. 

062 

"     28 

4-45     " 

15 
15 

14.0 

99 

Sh.  05m. 

9604 

5  ooo 

A. 

086 

"     3 

1  1.  06  A.M. 

16 

20.5 

146    .... 

58m. 

i  219!    336 

087 

"     3 

2.29  P.M. 

16 

14.0 

99    .... 

4h.  2im. 

4  82g!     613 

098 

Feb. 

12.24      " 

17 

20.  o 

142    

2h.  oSm. 

2  848      326 

01 

" 

2.48      " 

17 

13.0 

92    .... 

4h.  32m. 

5  508      102 

05 

" 

5.07      ' 

17 

16.0 

113    .... 

6h.  Sim. 

7  528      135 

09 

"       3 

10.38  A.M. 

18 

25.0 

177    

38m. 

874      477 

12 

3 

1.20  P.M. 

18 

24-5 

174    .... 

3h.  2om. 

4774 

607 

14 

3 

3.26       " 

18 

25.0 

177    .... 

5h.  26m. 

7824 

492 

118 

3 

5.O2       " 

18 

21.5 

152    

7h.  O2in. 

10024 

600 

123 

"       4 

10.25  A.M. 

19 

24.0 

170    

39m. 

880  

126 

4 

11.52       " 

19 

25.0 

177    

2h.  o6m. 

2  920j  I  200 

129 

4 

2.36  P.M. 

19 

14.0 

99    • 

4h.  5om. 

6640 

990 

133 

4 

5   22       " 

19 

14.0 

99    

7h.  36m. 

9640 

255 

139 

5 

10.34  A.M. 

20 

22.  0 

156 

02  m. 

33 

404 

143 

5 

11.58       " 

20 

26.0 

.  184 

ih.  26m. 

2  143 

522 

147 

5 

3.17  P.M. 

20 

I8.5 

132 

4h.  45111. 

6553 

i  376 

152 

158 

5 
6 

5.12     " 

10.29  A.M. 

2O 
21 

ii.  5 
29.0 

82 
206 

6h.  4001. 
57m. 

8393 
i6ig 

442 

980 

159 

6 

12.  06  P.M. 

21 

20.  o 

142 

2h.  34m. 

3969 

i  024 

1  66 

"       6 

3.21       " 

21 

23.5 

1  66 

5h.  49111. 

8619 

2  040 

171 

"       6 

4.20      " 

21 

22.  O 

156 

6h.  48m. 

9959 

I  800 

176 

7 

10.25  A.M. 

22 

26.0 

184 

53m. 

i  340 

6OO 

1  80 

7 

1.40   P.M. 

22 

23.0 

163 

4h.  o8m. 

53<>° 

I  6OO 

181 

7 

3-37     " 

22 

23.O 

163 

6h.  O5m. 

7650 

700 

189 

"       8 

10.45  A.M. 

23 

22.0 

156 

ih.  27m. 

2054 

194 

8 

2.31   P.M. 

24 

25.O 

177 

2gm. 

744 

768 

197 

"       8 

4-56      " 

24 

2O.  O 

142 

2h.  54m. 

3524 

660 

205 

"       10 

10.27  A.M. 

25 

18.0 

128 

ih.  0301. 

1336 

1  66 

210 

"      10 

2.02   P.M. 

26 

20.  o 

142 

ih.  32m. 

2005      200 

214 

"        IO 

3.26       " 

26 

12.  O 

85 

2h.  56m. 

3575!     49i 

2ig 

"       10 

5.  H       " 

27 

Ig.O 

135 

ih.  14111. 

i  510  i  250 

224 

"     II 

10.24  A  M. 

27 

20.0 

142 

3h.  oim. 

2  540       376 

227 

"     II 

1.03   P.M. 

28 

2O.  O 

142 

ih.  5im. 

2653        151 

230 

"     II 

3.22      " 

29 

22.  O 

156 

56m. 

I  365        605 

234 

"     II 

5.18'    " 

29 

6.0 

42 

2h.  52m. 

3  595'     39° 

237 
239 

"       12 
"       12 

10.23  A.M. 
1.20  P.M. 

30 
30 

23.0 
I4.O 

163 
99 

ih.  osm. 
4h.  02m. 

i  426        62 
4  97&      &35 

240 

"       12 

3-13      " 

31 

24.5 

174 

ih.  ogm. 

i  522      252 

245 

"       12 

4-57      " 

31 

21.  O 

T49 

2h.  53m. 

3  802      4g8 

251 

"       13 

9.58  A.M. 

32 

21.0 

149 

23m. 

532        5& 

254 

'       13 

12.35    P.M. 

32 

23.0 

163 

3h.  oom. 

42121     117 

257 

'       13 

2.2g       " 

32 

22.  O 

156 

4h.  54m. 

6  782      505 

260 

'       13 

4-45     " 

32 

18.0 

128 

7h.  lorn. 

g652!     957 

268 

!  I4 

10.35  A.M. 

33 

22.0 

156 

ih.  I5m. 

1  668      227 

272 

1.26  P.M. 

33 

21.  O 

149 

4h.  o6m. 

5  288      132 

276 

"       14 

3-33     " 

33 

ig.o 

135 

6h.  ism. 

6  898      209 

278 

'       14 

4.56     " 

33 

I8.5 

132 

7h.  36m. 

8  488      296 

286 

'       15 

10.24  A.M. 

34 

27.0 

igi 

55m. 

i  402      580 

290 

'       15 

1.38   P.M. 

35 

24.0 

170 

o6m. 

93   i  085 

294 

'      15 

3.16       " 

35 

I4.O 

99 

ih.  44m. 

2  273    I  290 

299 

'     15 

5.27       " 

35 

Ig.O 

135 

3h.  55m. 

4  683      446 

305 

'      17 

IO.24  A.M. 

36 

25.0 

177 

5om. 

i  130      925 

3°9 

'      17 

1.48  P.M. 

36 

23.O 

163 

4h.  1401. 

5  910  i  025 

'      17 

3-35       " 

37 

24.0 

170 

o6m. 

155      44i 

315 

'      17 

5.  ii     " 

37 

22.  5 

1  60 

ih.  42m. 

2355      i°l 

323 

"      18 

10.38  A.M. 

37 

21.0 

149 

3h.  3gm. 

4  965   i  160 

327 

"      18 

12.07   P.M. 

37 

20-5 

146 

5h.  oSm. 

6  925      695 

331 

"      18 

2.34       " 

38 

24.0 

170 

3im. 

734      73° 

334 

"     18 

4-59     " 

38 

21.0 

149 

2h.  56m. 

4  084      848 

339 

"      18 

5-  ii      ' 

38 

21.0 

149 

3h.  o8m. 

4314      "9 

346  i            '     19 

10.27  A.M. 

38 

22.0 

151 

4h.  54m. 

6  444'     604' 

COMPOSITION  OF  OHIO   RIVER    WATER  AFTER   PURIFICATION. 
TABLK  No.  4. — Continued. 

Western    Piessure    System. 


'77 


R 

teof 

„• 

- 

Collected. 

Fill 

ration. 

Ix. 

jS 

io 

. 

u 

«  u 

Period  of 

J  t* 

^ 

1 

Number 

0. 

JS.  _ 

•a 

Service  Since 
Last 

s  i  s 

b  £' 

e 

of 

£  . 

"•^  u  ^ 

£ 

Washing. 

•s  £  ^ 

a  w 

Remarks. 

\ 

Date. 

Hour. 

Run. 

ul 

1:1 

? 

Hours  'ind 
Minutes. 

las 

ll 

•c 

•f  2 

—  a" 

£ 

1.33 

Uf/j 

« 

(_> 

S 

j 

h. 

03 

1896 

1350 

Feb.   ig 

11.43  A.M. 

38 

20.  0 

142 

6h.  lom. 

8804 

51300 

A. 

1354 

"       19 

3.13   P.M. 

39 

23-5 

166 

2h.  4gm. 

3  980 

595 

1356 

19 

4-59     " 

39 

24.0 

170 

4h.  35m. 

6540 

442 

1365 

20 

11.15  A.M. 

40 

25.0 

177 

I3m. 

258 

197 

1374 

"         2O 

1.23   P.M. 

40 

24-0 

170 

2h.  2im. 

3498 

305 

1380 

"         20 

3.25      " 

40 

22-5 

1  60 

4h.  23m. 

6278 

745 

1384 

"         2O 

5.08      " 

40 

ig.o 

135 

Gh.  o6m. 

8  298 

881 

1392 

"         21 

10.07  A.M. 

41 

20.5 

146 

3Sm. 

1658 

77 

1397 

"         21 

12.52   P.M. 

41 

23.0 

163 

3h.  23m. 

4388 

MS 

1400 

"         21 

3-13       " 

41 

18.5 

132 

5h.  44m. 

7  208 

401 

1403 

"         21 

5-01       ' 

42 

25-5 

1  80 

ih.  24m. 

2  103 

53 

1420 

24 

10.22  A.M. 

42 

23.0 

163 

3h.  ism. 

4490 

187 

1426 

"        24 

1.30    P.M. 

42 

22.0 

6h.  23m. 

9030 

848 

1429 

"        24 

3  31       " 

43 

24-5 

174 

56m. 

I  316 

338 

1434 

24 

5.24      ' 

43 

23.0 

163 

2h.  4gm. 

3956 

615 

1440 

25 

10.38  A.M. 

43 

25-0 

177 

4h.  33m. 

6266 

I  205 

1444 

25 

1.23    P.M. 

43 

22.0 

156 

7h.  i8m. 

10066 

I  510 

1448 

25 

3.18       " 

43 

21.5 

152 

gh.  1  3m. 

12  556 

720 

1449 

"     25 

4-53     " 

43 

16.0 

"3 

zoh.  4Sm. 

14456 

368 

«459 

"     26 

10-34  A.M. 

44 

21.0 

149 

ih.  I2m. 

I  602 

205 

1463 

"     26 

12.2O   P.M. 

44 

25-0 

177 

.    .. 

2h.  58m. 

4272 

595 

1465 

"     26 

3.II       " 

44 

25.0 

177 

5h.  4gm. 

85I2 

650 

1469 

'•     26 

5-15       " 

44 

25-0 

I  So 

7h.  53tn. 

II  602 

645 

1475 

"       27 

IO.28  A.M. 

44 

24-5 

174 

gh.  25m. 

13  702 

887 

1482 

27 

1.50    I'.M. 

44 

16.0 

"3 

I2h.  47111. 

17  Sl2 

618 

1486 

"       27 

3-<-9     " 

45 

32.0 

227 

59111. 

'493 

99" 

M9I 

"     27 

5-25     ' 

45 

26.0 

184 

3h.  15111. 

5  213 

212 

'499 

"     28 

10.48  A.M. 

45 

30.0 

213 

5h.  oSm. 

8033 

3<J5 

1504 

"     28 

3  29  P.M. 

45 

24.0 

170 

gh.  4gm. 

15  123 

710 

1506 

28 

5.00       " 

45 

20.  0 

142 

Ilh.   20II1. 

17243 

583 

1514 

"       2g 

10.40  A.M. 

45 

25-5 

I  So 

I2h.  48111. 

19433 

443 

1519 

29 

1.42    P.M. 

45 

23.0 

163 

I5h.  50111. 

23713 

I  7<x) 

1523 

29 

3-25     " 

45 

21.5 

152 

I7h.  33111. 

25953 

I  140 

1526 

1       29 

5.08     " 

45 

21.0 

149 

igh.  i6m. 

28043 

33" 

1535 

Mar.     2 

9.50  A.M. 

46 

25-0 

177 

22m. 

492 

Sio 

1539 

2 

10.30       " 

46 

25-5 

1  80 

ih.  O2m. 

I  502 

1543 

"            2 

I  42   P.M. 

46 

27.0 

191 

4h.  I4m. 

6  162 

i  475 

1547 

2 

3-22       " 

46 

24-5 

174 

5h.  54m. 

8722 

6000 

1552 

"            2 

5.16       " 

46 

25.0 

177 

7h.  48m. 

II  462 

720 

1560 

3 

10.48  A.M. 

46 

25-5 

i  •., 

gh.  som. 

14342 

I  600 

1562 

3 

12.52    P.M. 

46 

25-5 

1  80 

nh.  54m. 

17452 

74" 

1567 

3 

3-16       " 

46 

20.0 

142 

I4h.  i8m. 

20  982 

410 

1573 

3 

5.19       " 

46 

22.5 

160 

i6h.  2im. 

23  922 

442 

1579 

4 

10.53  A.M. 

46 

20.il 

142 

iSh.  25m. 

26772 

940 

1583 

4 

1.04   I'.M. 

46 

22-5 

1  60 

2oh.  36111. 

29  722 

683 

I  ;  "  7 

4 

3-24      " 

47 

24.5 

174 

3gm. 

970 

222 

1592 

4 

5.oS      " 

47 

24.5 

'74 

2h.  23m. 

4  260 

605 

1598 

5 

10.44  A.M. 

47 

27.0 

191 

4h.  2gm. 

6180 

I  040 

1602 

5 

12.59  I'.M. 

47 

25.0 

177 

6h.  44m. 

9520 

705 

if,.  ,7 

5 

3.26     " 

47 

23.O 

163 

gh.  nm. 

12  980 

345 

1609 

5 

5.07    " 

47 

25.0 

177 

loh.  52m. 

15420 

370 

1619 

6 

10.40  A.M. 

47 

23.0 

163 

I2h.  55m. 

1  8  140 

231 

1624 

"         6 

12.45    I'.M. 

47 

23-5 

1  66 

I5h.  oom. 

20  960 

105 

1629 

6 

3.26       " 

47 

2f).O 

184 

I7h.  4im. 

24  620 

585 

1630 

6 

5.19       " 

47 

26.0 

184 

igh.  34m. 

27  460 

385 

1640 

7 

10.52  A.M. 

48 

28.0 

igg 

52rn. 

I  230 

845 

1643 

7 

12.59   I'.M. 

48 

25.0 

177 

2h.  sgm. 

4  530 

280 

1646 

7 

3.I6      " 

48 

25-5 

1  80 

5h.  i6m. 

76.00 

435 

if,;  | 

7 

5-25      " 

48 

24.O 

170 

7h.  25m. 

10760 

320 

1659 

9 

II.  Og  A.M. 

48 

22.5 

160 

gh.  3gm. 

13930 

212 

1660 

g 

9.  CO  A.M.   to  3.25    P.M. 

48 

23   -O 

16-5 

1664 

9 

12.58    I'.M. 

48 

25-5 

*  vj 
1  80 

nh.  28m. 

16310 

235 

1665 

0 

1.2S       " 

48 

24.0 

170 

I3h.  55.11. 

19710 

;;  = 

WATER  PURIFICATION  AT  LOUISVILLE. 
TABLE    No.    4. — Continued. 

Western     Pressure    System. 


£> 

B 

3 

y. 

Collected. 

Number 

R;i 
FiHr 

s. 

kt; 

la 
u 

eof 

=  °-  . 

-  £  = 
=  <£ 

a0"1 

rt 

X 

1 

_] 

Period  of 
Service  Since 
Last 
Washing. 
Hours  and 
Minutes. 

y.  . 

u  &D 

sy 

.•=  JU 

u. 

'.£ 

<J  .  • 

«8 
n 

Remarks. 

Date. 

Hour. 

1675 
1681 
1685 
1690 
1696 
1701 
1705 
1709 
1666 
1716 
1722 
1726 
I73T 
1736 
1742 
1746 
1750 
1755 
1762 
1763 
1768 
1769 
1774 
1775 
1781 
1788 
1789 
1794 
1795 
1800 
1801 
1806 
1814 
1815 
1820 
1821 
1826 
1827 
1828 
1838 
1839 
1844 
1845 
1851 
1865 
1869 
1877 
1883 
1891 
1897 
1903 
1909 
1915 
1921 
1924 
1930 
I93« 
1943 
1949 
1950 
1960 
1963 
1966 

1896 
Mar.  9 
"   10 
"   10 

"    10 

"   10 
"   I 

"   i 

"  9-1 
I 

"    12 
"    12 
"    12 
"    12 
"    13 
13 
13 
."    13 
14 
M 
M 
'4 
M 
14 
"    14 

"   16 
"   16 
"   16 
"   16 
16 
"   16 
"   16 
"   '7 
"   l~ 
"   T7 
"   17 
J7 
17 
"   17 
"   IS 
"   18 
"   18 
"   18 
"   18 
"   J9 
19 
'9 

19 

20 
"    2O 
"    2O 
"    20 
"    21 
"    21 
21 
"    21 

"    23 
i    23 

'    23 
'    23 
'    24 
:    24 
'    24 

5.12  P.M. 
1O.28  A.M. 
1.40  I'.M. 
3.16   " 
5.20   " 
IO.25  A.M. 
1.36  I'.M. 

3-27  " 

3.25  P.M.  to  3.27  P.M. 
S.lg  P.M. 
10.25  A.M. 
1.02  I'.M. 

3-33  " 
5.20  " 

10.31  A.M. 
I.I7  I'.M. 
3-21   " 
5.06   " 
10.40  A.M. 
9.30  A.M.  to  10.40  A.M. 
I.I3  I'.M. 
10.40  A.M.  to  I.I3  I'.M. 
1.43  P.M.  "  3.18   " 
3.18  I'.M. 

4-55  " 

9-OO  A.M. 
10.37   " 
10.37  A.M.  to  1.20  I'.M. 
I.2O  I'.M. 
1.  2O  I'.M.  to  3.22  I'.M. 
3.22  I'.M. 
5.09   " 

9  22  I'.M.  to  TO  3;  A.M. 

10.35  A  M. 
10-35  A.M.  to  1.20  I'.M. 
I.  2O  I'.M. 
1.  2O  I'.M.  to  3.25  I'.M. 
3.25  P.M. 
5-07   " 

10.34  A.M. 

9.25  A.M.  to  10.34  A.M. 

1.19  P.M. 

10.34  A.M.  to  I.I?)  P.M. 
I.I9  I'.M.  "   3.30  " 
9.30  A.M.  "  10.53  A.M. 
10.53   "    "  12.20  P.M. 
12.  2O  P.M.  "   3.  II   " 
3-II   "    "   5.30   " 
9.00  A.M.  "  10.35  A.M. 
10.35   "    "   I.I5  P.M. 
I.I5  P.M.  "   3.37   " 

3-37  '   "  5.30  " 

10.48  A.M. 
1.28  P.M. 
3-27   " 
5-07   " 
g.OO  A.M.  to  10.30  A.M. 
10.30   "   "  12.05  P.M. 
12.05  P-M.  "   3.05   " 
3.05   "   "   4.00   " 
9-00  A.M.  "  11.30  A.M. 
11.30   "   "   2.30  P.M. 
2.30  P.M.  "   5.30  " 

48 
49 
49 
49 
49 
49 
49 
49 
49 
49 
49 
49 
49 
49 
50 
50 
50 
50 
50 
50  • 
50 
50 
50 
50 
50 
50 
5o 
50 
50 
50 
50 
50 
51 
5i 
51 
51 
51 
51 
5i 
51 
51 
51 
51 
51 
52 
52 
52 
"   52 
52-53 
53-54 
54 
55 
56 
57 
57 
57 
58 
58 
58-59 
59 
60 
60-61 
61 

24.0 

22.5 
24.0 
25.0 
24.0 
25.5 
23-5 
23.0 
22.9 
24.0 
25.0 
24.0 

22.0 
22.  0 
2J,.O 
23.O 
24.0 
22.  O 
23-5 
22-5 
23.0 
23.0 
23.2 
24-0 
24.0 
21.6 

23.0 
23-3 
23-0 
23.7 
24.0 
23.0 
23.4 
23.5 
23.2 
23.0 
23.2 

22.  5 
22.5 
22.0 
22  6 
23.0 
22.  f) 
21.0 
25.0 
21.2 
21.8 

iS.s 
19-3 
16.5 
16.3 
ig-5 

iS.o 
18.5 
13-5 

II.  O 

18.4 
17.0 
16.8 
19.3 
21.4 
J9-7 
n.- 

170 
1  60 
170 
177 
170 
i  so 

1  66 
163 
162 
170 
177 
170. 
156 
156 
170 
163 
170 
156 
1  66 
1  60 
163 
164 
164 
170 
170 
131 
163 
165 
163 
168 
170 
,63 
1  66 
1  66 
164 
163 
164 
1  60 
.  160 
156 
1  60 
163 
156 
M9 
177 
149 
155 
134 
'37 
116 
US 
138 
128 
132 
96 
78 
131 
1  2O 
119 
137 
152 
140 
98 

I5h.  42m. 
ih.  I2m. 
4h.  24m. 
oh.  oom. 
8h.  04m. 
gh.  39111. 
I2h.  I2tn. 
14)1.  O3m. 

22  090 

1618 
6398 

8  788 
ii  778 
1-5868 
17438 
19938 

175 
330 
125 

20J 
225 
199 
165 

182 

C. 

C. 
C. 

C. 
C. 

c. 

C. 

c. 

c. 

I5h.  55"'- 
I7h.  35m. 
2oh.  oSm. 
22h.  39111. 
24)1.  26111. 
ih.  nm. 
3h.  57111. 
6h.  oim. 
7h.  46,11. 
gh.  5om. 

22  518 
24738 
28  418 
32058 

34588 
I  693 
5603 
8423 
10863 
13  633 

129 
430 
298 
565 
195 
181 
194 
163 
no 

177 
225 
139 
205 
98 
187 
132 
274 
3f>5 
38. 
322 
395 
305 
480 
505 
685 
500 
i  go 
118 
185 
420 
765 
425 
280 
250 
325 
450 
97<- 
780 

I  OOO 

500 

400 
500 

800 
890 
980 

I  050 

I  430 

i  "5 
I  105 

780 
740 
297 
500 
58c 

.  .  .  .  I2h.  23111. 

17  173 

I4h.  28m. 
l6h.  osm. 

20  083 
22333 

....  iSh.  17111. 

25  243 

....  2ih.  com. 

29  043 

•  •  •  •  23)1.  O2m. 
;  24h.  49111. 

31  933 
34  223 

....   ill  19111. 

1843 

4h.  O4tn. 

5  663 

6h.  oqm. 
~h.  5im. 
gh.  48111. 

8  563 
10853 
13  543 

I2h.  33m. 

17  263 

ih.  28m. 
iSm. 

2h.  17111. 
3h.  57m. 

i  580 
335 
2085 

3275 

COMPOSITION  OF  OHIO   RIVER    WATER   AFTER   PURIFICATION. 


179 


TABLE  No.  4. —  Continued. 


Western     Pressure    System. 


Collected. 

Ra 

Fill 

t<   ol 

£ 

8 

5 

« 

a; 

'     • 

Period  of 

*"   1? 

3 

Serial  Numbc 

Date. 

Hour. 

Number 

Run. 

u| 

H 
U 

I0" 
<^t 

o  UI 

=  &.? 

S 

X 

- 

ServiceSince 
Last 
Washing 
Hours  and 
Minutes. 

^lo 
fc.  tr^ 

153 

i 

«a 

'E'~ 
^u 
M 

Remarks. 

1896 

6  1   62 

208 

12    6 

80 

28-? 

6-3  6  i 

16  o 

06 

66 

1  1   g 

825 

009 

J 

6-7 

"        26 

t. 

* 

"        26 

63 

I  6     Z 

16 

"        26 

"* 

"        26 

fin 

!_i     g 

26 

26 

1  6   i 

3 

"        26 

TCg 

2059 
2060 
2061 
2062 
2063 

"    27 
27 
••    27 
27 
27 

2.30  A.M. 
2-45      " 
2-59      " 
3.2O      " 
3-30      " 

71 

7' 
71 
72 
72 

17.0 
17.0 
i6.5 
17.0 
17.0 

16  3 

20 

20 

16 

20 
20 

5h.  lom. 
5h.  25171. 
5h.  3901. 
O2m. 
I2m. 

5  202 
5452 
5  662 
37 
217 

290 
300 
400 
425 
IS9 

E. 
E. 
E. 

The  series  of  results  on 
run  No.  72  was  used  in 

2of)8 

2069 
2070 
2071 
2072 
2073 
2074 

"    27 
27 
1    27 
!    27 
27 
27 

5-50      " 

6.00      ' 
6.  10    " 
6.50    " 
7.20    " 

8.20      " 

72 

72 

72 
72 

72 

19.5 
19.0 
18.5 
17-5 
17-5 
16.5 

38 

35 
32 
24 
24 
16 
26 

33m. 
43m. 
53m- 
ih.  33m. 
2h.  0301. 
3h.  0301. 

687 
807 
987 
1667 
2  217 
3187 

189 
295 
470 
190 

185 
260 

but  not  for  the  day. 

2079 
2080 

"    27 
27 

9.20  A.M. 
IO.2O      " 

72 

72 

17.0 
16.0 
16  6 

20 
13 

4h.  03m. 
5h.  03m. 

4237 
5  151 

305 
405 

2085 
2086 
2087 
2088 
2089 
2090 
2091 
2092 
2093 
2094 
2095 
2096 
2097 

••    27 
11    27 

..         27 
..         27 
'         27 

"         27 

27 

27 

"       27 

:     27 

27 

27 

"     27 

I  1.30  A.M. 
12.  10  I'.M. 
12.20      " 
12.30      " 
I2.4O      " 
12.50      " 
I.OO      " 
I.IO      " 

1.  20    '* 

1.30  " 
1.40   " 
1.50   " 

2.OO      " 

-2 
72 
72 

72 

72 
72 
72 
72 

72 

72 
72 
72 
72 

16.0 
16.0 
15-5 
15-5 
15-5 
15-5 
15-5 
15.5 
15-5 
15.0 
15-0 
15-0 
15.0 
15  8 

'3 
13 
IO 
IO 
IO 
10 
IO 
10 
IO 

06 
06 
06 
06 

6h.  I3m. 
6h.  53111. 
7h.  03111. 
7h.  I3m. 
7h.  23m. 
7h.  33m. 
7h.  43m. 
7h.  53m. 
8h.  03m. 
8h.  I3m. 
8h.  23m. 
8h.  33m. 
8h.  43m. 

6417 
6897 
7057 
7217 
7367 
7517 
7681 
7837 
7987 
8147 
8297 
8447 
8607 

342 
302 
257 
3'7 
266 
3°5 
370 
408 
360 
270 
309 
285 
345 

685 

26 

u8 

16  6 

1  66 

"       27  28 

17  8 

08 

28 

28 

5  30     "      "     8  30    " 

"      28 

18  I 

28 

28 

Tfi  9 

28 

5.30     "      "     8  30    " 

76 

A  •> 

28 

4j' 

2(1 

2  I  (  )  2 

"        2q 

2.30  A.M.    "       5.30     " 

77-78 

15.  q 

12 

7.12 

WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  4. — Continued. 

Western     Pressure    Systei 


3 

e 

z 

1 

2166 
2170 
2174 
2175 
2176 
2177 
2178 
2179 
2183 
2186 
2190 
2193 
2197 

2200 
2204 
2208 
2211 
2217 
2221 
2225 
2230 
2235 
2238 
2243 
2248 
2251 
2256 
2259 
2263 
2268 
2272 
2278 
2282 
2287 
2290 
2295 
2300 
2303 
2768 
2775 
2781 
2787 
2795 
2799 
2805 
2806 
28og 

a8ii 

2815 
2819 
2822 
2827 
2831 
2858 
2868 
2874 
2876 
2882 
2886 
2893 
2897 
2901 
2906 

Collected. 

Number 
Run. 

Rale  of 
Filtration. 

£ 
i 

j 

Period  of 
ServiceSince 
Last 
Washing. 
Hours  and 
Minutes. 

e 

|.|L 

i|£ 

lA 
it 

3 

u  u- 
!Tg 

F 

Remarks. 

S. 

!§ 

U 

osS, 

o^S 

_0.N 

Date. 

Hour. 

1896 
IMar.  29 
"       29 
'       29 
29 
29 
;       29 
29 
29 
:       29 
29 
1       29 
'       29-30 
'       30 
30 
30 
1       30 
1      30 
1      3i 
:      3i 
1      3i 
April     i 

"         I 

"            2 
"           2 
"            2 
3 

3 
3 
4 
4 
4 
6 
6 
6 
7 
7 
7 
May     7 
7 
8 
8 
8 
8 
"        8-9 
9 
9 
9 
9 
9 
II 
"       II 
"       II 

"         12 
"         12 
"        12 
"         12 
13 
13 
13 
13 
14 
14 

5.30  A.M.  to     8.30  A.M. 
8.30      "       "  11.30      " 
11.30      "        "      2.30   P.M. 
3.26    P.M. 
3-32       " 
3-42       ' 

3-57     ' 
4.12     " 

2.3O  P.M.    to      5.30   P.M. 
5.30       "        "      8.30       " 
8.30       "         "11.30       " 
11.30      "        "      2.  30  A.M. 
2.30  A.M.    "      5.30      " 
5.30      "        "     8.30      " 
8.30      "        "   11.30      " 
11.30      "        "      2.30  P.M. 
2.30  P.M.    "     5.30      " 
9.30  A.M.     "   II.  30  A.M. 
11.30      "        "      2.30  P.M. 
2.30  P.M.    "      5.30      " 
9.30  A.M.    "   II.  30  A.M. 
11.30      "        "      2.30   P.M. 
2.30  P  M.    "      5.30      " 
9.40      "        "  II.3O  A.M 

73 
78-79 
79 
So 
80 
80 
80 
So 
80 
So 
80-81 
81 
81-82 
82 
82-83 
83 
83 
84 
84 
85 
86 
86-87 
87 
88 

15-3 
16.4 
16.4 
21.0 
2O.  O 
17-0 
I6.5 
16.0 
l6.g 
15-7 
i6.g 
17.1 

17-3 
15  fj 

09 
16 
16 

323 

i  686 
i  315 
635 
i  055 
355 
95 
109 
2475 
715 
i  056 
2985 
5950 
1585 
•i  725 
i  265 
i  145 
885 
i  455 
2545 
I  IIO 

9f>5 
i  025 
630 
i  no 
525 
i  185 
I  160 
475 
175 
198 
182 
57 
85 
130 
64 
7i 
94 

28g 
126 

20 
113 
91 

c. 
c. 
c. 
c. 
c. 

From    May     7-9      inclu 
sive,  the  results  of  both 
single       samples    and 
those  collected  by  the 
sampler  were  used  to 
obtain      the     average 
bacteria  for  days  and 
for  runs. 
C. 

C. 

49 

42 
20 
16 
13 
J9 
II 
119 

121 
122 

14111. 
2om. 
3Om. 
45m. 
ih.  oom. 

304 
404 
564 
804 
1054 

14.1 
14.7 
14-3 
15.9 
13.0 
11.7 
17.0 
16.1 
15-5 

99 
I03 
IOO 

"3 
92 

83 

120 

"3 
no 

1  08 

2.30  P.M.    "      5.30      " 
9.30      "        "   11.30  A.M 
II.  3O  A.M.    "      2.30  P.  M 
2.30  P.M.    "      5.30      " 
9.30      "        "   II.3O  A.M 
II.  30  A.M.    "      2.30   P.M 
2.30  P.M.    "      5.30      " 
9.30      "        "   11.30  A.M 
11.30  A.M.    "      2.30  P.M 
2.30  P.M.    "     5.30      " 
9.30      "        "   II.3O  A.M 
11.30  A.M.    "      2.30  P.M 
2.30  P.M.     "      5.30      " 
3.2O  P.M. 
g.20      " 
3.05  A.M. 
g.OO      " 

g.oo  A.M.   to   3.30  P.M 

3.00  P.M.     "      9.00       " 
g.OO       "         "      3.00       " 
3.OO  A.M. 
3.00  A.M.    to    8.30  A.M 
g.OO  A.M. 
1.  2O  P.M. 
3-27      " 
IO.OO  A.M.    to     1.55   P.M. 
3.OO  P.M. 
9.00       " 
3.00  A.M. 
g.OO      " 
12.00  M. 
8.30  P.M. 
2.OO  A.M. 
8.00       " 
1.  00  P.M. 
7.00  P.M. 
3-OO  A.M. 
9.00       " 

89 
go 
go 
91 
91 
91-92 
92 
93 
93 
93 
94 
94 
94 
95 
96 
96 
96 
96-97 
97 
97 
97 
97-98 
98 
98 
98 
99 
99 
99 

IOO 
IOO 
101 
101 
IO2 
103 
102 
103 
103 

i  "4 

14.7 
17.0 
13.0 
15-8 
16.0 
16.0 
14.6 
19.2 
18.4 
16.6 
18.9 
18.8 
17-7 
23.5 
23.5 
24.0 

22.0 
22.6 
22.2 
22.2 
23.0 
23.3 
22.5 
23.5 
23.0 
23-4 
23-5 
22.  O 
24.0 
1'4.  < 
23.0 
22.0 
24.0 
23-5 
23.0 
24.0 
23-5 
23.5 

104 
1  20 
92 

112 
"3 
113 
103 
136 
131 
"7 
134 
137 
125 
166 
1  66 
170 
156 
161 
156 
156 
163 
164 
1  60 
166 
163 
165 
1  66 
156 
170 
170 
163 
156 
170 
166 
163 
170 
1  66 
1  66 

6h.  2om 
0701 
5h.  52m 
nh.  47m 

8  870 
128 
7988 
16378 

I5h.  O5m. 

20023 

253 

171 

346 

225 
230 
363 
287 

1  80 
219 
242 
278 
219 
93 
115 
171 
152 
156 
132 

4h.  56m. 
gh.  i6m. 
nh.  23m. 

6973 
13033 
15943 

5h.  2im. 
nh.  2im. 
5h.  03m. 
lib.  O3m. 
ih.  5gm. 
loh.  2gm. 
3h.  36m. 
gh.  36m. 
I4h.  36m. 
3h.  57m. 
nh.  57m. 
4h.  3om. 

7497 
5637 
7  oio 
15  280 
2683 
14  154 
5  ooi 

13  121 

19731 

5  5oi 
16425 
6443 

COMPOSITION  OF  OHIO  RIVER    WATER   AFTER   PURIFICATION. 


181 


TABLE    No.    4. — Continued. 

Western    Pressure    System. 


Rate  of 

~ 

g 

Collected. 

Filtration. 

£ 

il 

.a 

^ 

~^ 

»>  i- 

Period  of 

u  g> 

3 

w 

Number 

a 

I  °- 

•a 

Service  Since 

w's  ~ 

u 

s 

z 

of 

Is 

Cos 
~  <  o 

X 

Washing. 
Hours  and 

!1! 

V  ?• 

Remarks. 

Date. 

Hour. 

.s.E 

° 

Minutes. 

£  si 

ii 

'I 

u 

!*" 

3 

£ 

lu 

1896 

2gio 

May  14 

2.0O  P.M. 

104 

23.0 

163 

gh.  3om. 

13813 

131 

2gi6 

"  T4 

8.00  " 

105 

24.0 

170 

3h.  34m. 

5  igo 

136 

2g2o 

"  15 

1.  00  A.M. 

105 

23.5 

1  66 

8h.  34m. 

12  380 

181 

2924 

'  15 

8.00  " 

1  06 

23.0 

163 

3h.  4om. 

4978 

222 

2928 

'  15 

11.00   " 

106 

26.0 

184 

6h.  4om. 

g268 

237 

2934 

'  15 

5.21  P.M. 

I  Of) 

18.0 

128 

I2h.  iSm. 

17  705 

700!  Wasting  2  min.,  66  cu.  ft. 

2935 

'  15 

5.24  •' 

1  06 

19.0 

135 

I2h.  i8m. 

17705 

705    "    5  "  106 

2936 

'  15 

5.27  " 

1  06 

22.  O 

156 

I2h.  i8m. 

17705 

216 

8  "  166 

2937 

'  15 

5.31  ' 

107 

ig-S 

138 

02  m. 

53 

115 

2938 

'  15 

5-33  " 

107 

24.0 

179 

04111. 

113 

151 

2939 

'  15 

5-35  " 

107 

24.0 

170 

o6m. 

153 

170 

2940 

'  '5 

5-37  ' 

107 

24.0 

170 

08  m. 

203 

134 

2941 

'  15 

5-39  " 

107 

24.0 

170 

lorn. 

253 

122 

2942 

'  15 

5.41  ' 

107 

24.0  170 

I2m. 

293 

102 

2943 

'  15 

5-43  " 

107 

24.O  I7O 

1401. 

333 

71 

2944 

'  15 

5-45  ' 

107 

24-0  170 

i6m. 

383 

54 

2945 

'  15 

5-47  ' 

107 

24.0  170 

i8m. 

443 

105 

2946 

'  15 

5-49  " 

107 

24-5   174 

zom. 

493 

70 

2947 

'  15 

5.51  ' 

107 

24.5  174 

22m. 

523 

68 

2948 

'  15 

5-53  " 

107 

24-5  174 

24m. 

573 

82 

2949 

'  15 

5-55  " 

107 

24.5  174  

26m. 

623 

70 

2950 

'  15 

5-57  " 

107 

24.5  174  

28m.    673 

82 

2951 

'  15 

5-59  " 

107 

24-5 

174 

3"m-    703 

56 

2952 

'  15 

6.04  ' 

107 

24-5 

174 

35m.    843 

66 

2954 

'  15 

6.14  " 

107 

24-5 

174 

45m. 

I093 

74 

2955 

'  15 

6.29  " 

107 

24-5 

174 

ih.  oom. 

M33 

81 

2956 

'  15 

7.29  " 

107 

24-5 

174 

2h.  oom. 

2863 

65 

2957 

'  15 

8.2g  " 

107 

24.5 

174 

3h.  oom. 

4303 

85 

2958 

'  15 

9.29  " 

107 

24.0 

174 

4h.  oom. 

5733 

99 

2959 

'  15 

10.29  " 

107 

24-5 

174 

5h.  oom. 

7  "3 

go 

2962 

'  15 

11.00   " 

107 

25.0  177 

5h.  3im. 

7873 

142 

2964 

"   16 

12.29  A.M. 

107 

24.0 

170 

7h.  oom. 

10  033 

f'5 

2965 

"  16 

1.29   " 

107 

24-5 

'74 

Sh.  oom. 

n  623 

400 

2gf>6 

"  if) 

2.29   " 

107 

23-5 

1  66 

gh.  oom. 

I2gi3 

i2g 

2967 

"   16 

3.29   " 

107 

24.0 

170 

loh.  oom. 

14  293 

71 

2968 

"   If) 

4-2g  " 

IO7 

1  1  h  .  oom  . 

15  813 

200 

2971 

"  16 

5.00  " 

107 

24.0 

170 

nh.  3im. 

16703 

122 

2972 

"  16 

5-2g  " 

107 

24.0 

170  

I2h.  oom. 

17263 

log 

2974 

"  16 

6.2g  " 

107 

23-5 

166  .... 

I3h.  oom. 

18753 

108 

2975 

"   16 

7.29  " 

107 

24.0 

170  

I4h.  oom. 

20133 

go 

2976 

"  16 

8.29  " 

107 

24.0 

170  

I5h.  oom. 

21  523 

go 

2979 

"  16 

9-29  " 

107 

22.5 

160  .  .  . 

i6h.  oom. 

22983 

81 

2982 

"  16 

IO.OO   " 

107 

23.0 

163  .... 

i6h.  3im. 

23  6g3 

91 

2983 

"  16 

10.  29  " 

107 

23.0 

163  .... 

I7h.  oom. 

24  363 

63 

2984 

•'  16 

11.29  " 

107 

23-5 

166  

i8h.  oom. 

25753 

98 

2985 

"  16 

12.29  '".M. 

107 

23.0 

163  .... 

igh.  oom. 

27  173 

161 

2986 

"  16 

1.29  " 

107 

23.0 

163  .... 

2oh.  oom. 

28573 

136 

2987 

"  16 

2.29  " 

107 

23.0 

163  .... 

2ih.  oom. 

29  933 

127 

2993 

"  16 

3.00  " 

107 

22.5 

160  .... 

2lh.  3im. 

30673 

151 

2994 

"  16 

3.29  " 

107 

23.0 

163  .... 

22h.  oom. 

31403 

142 

2998 

"  18 

12.00  M. 

1  08 

14-5 

102   2.3 

2h.  45m. 

2  406 

I  1  20 

3001 

"  18 

2.48  P.M. 

1  08 

14.0 

99  4.6 

5h.  33m. 

4826 

429 

3oog 

"  18 

6.07   " 

1  08 

15.0 

106   7.0 

6h.  57m. 

6086 

265 

3011 

"  18 

g.OO   " 

108 

15.0 

106   4.7 

gh.  som. 

8706 

3000 

3016 

"  18 

[2.(X>   " 

1  08 

'5-5 

1  10 

7.0 

I2h.  <om. 

II  466 

198 

3019 

"  19 

3.00  A.M. 

108 

'4-5 

1  02 

14-7 

I5h.  5om. 

14096 

185 

3025 

'  '9 

6.00   " 

1  08 

15-5 

no 

12.3 

iSh.  5001. 

16786 

215 

3028 

'  19 

8.30   " 

108 

16.0 

113  10.0 

2ih.  2om. 

I8gi6 

'95 

3033 

'  '9 

I2.O8  P.M. 

1  08 

14.5 

102  20.  8 

24h.  58m. 

22046 

208 

3038 

'  19 

3-05   " 

1  08 

15.0 

106  20.  8 

27h.  55m. 

24606 

300 

3042 

'  19 

6.00  " 

1  08 

14.0 

99 

18.5 

3oh.  som. 

27086 

539 

3043 

'  19 

9.00  " 

1  08 

14.0 

99 

18.5 

33h.  5om. 

2gs86 

420 

3049 

'  '9 

12.  OO   " 

1  08 

14.0 

30.0 

36h.  5om. 

32073 

582 

WATER  PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  4. —  Continued. 
Western    Pressure    System. 


Ra 

e  of 

S 

u 

Collected. 

Filtr 

ation. 

£ 

il 

.H 

jj 

~~i; 

l/Tu 

Period  of 

V.  *• 

a 

ji 

Number 

a 

§  Q. 

•o 

ServiceSince 

i  •-  ~ 

LJ  v- 

3 
Y. 

Date. 

Hour. 

Run. 

ul 

!li 

°  ul 

X 

Last 

Washing. 
Hours  and 
Minutes. 

*|^ 
*-  tnS 

i>  c 

Remarks. 

5 

'?'?• 

~  a.  rf 

0 

-  JU 

"Cj 

in 

u 

Z 

*1 

tu 

n 

3054 

1896 
May  20 

3.00  A.M. 

108 

15.0 

1  06 

27-7 

3gh.  som. 

34726 

68 

3058 

"   20 

6.OO   " 

108 

14.0 

99 

27-7 

42  h.  som. 

37  246 

235 

3061 

"  20 

8.30   " 

08 

14.0 

99 

30.0 

45h.  2om. 

39  266 

242 

3063 

"  20 

9-43   " 

09 

15.0 

106 

2-3 

o6m. 

73 

340 

3065 

"   20 

9-53   " 

09 

14-5 

102 

2-3 

i6m. 

233 

165 

3070 

"  20 

12.  OO  M. 

09 

14.0 

99 

10.3 

2h.  23m. 

2  103 

310 

3073 

"   20 

3.0O  P.M. 

09 

14.5 

IO2 

4-7 

5h.  23111. 

4813 

190 

3078 

'   20 

6.OO   " 

09 

14.5 

102 

7-0 

8h.  23m. 

7353 

159 

3083 

"   2O 

q.OO   " 

09 

14-5 

102 

7.0 

nh.  23m. 

9883 

146 

3'>87 

"   2O 

12.00   " 

09 

14.0 

99 

ii.  6 

I4h.  23m. 

12  193 

144 

3090 

"   21 

3.00  A.M. 

09 

14.0 

99 

16.3 

I7h.  23m. 

I4&93 

"3 

3094 

"   21 

6.00  " 

09 

14.0 

99 

18.5 

2oh.  23m. 

17093 

139 

3099 

"   21 

8.30  " 

09 

13.5 

88 

19.6 

22h.  53m. 

19  133 

135 

3102 

"   21 

12.00  M. 

09 

14.0 

99 

23.1 

26h.  23m. 

22083 

162 

3109 

"   21 

3.06  P.M. 

09 

14-5 

102 

27.8 

29h.  29m. 

24733 

183 

3"3 

"   21 

6.00   " 

09 

14.5 

IO2 

32.4 

32h.  23m. 

27223 

99 

3116 

"   21 

g.OO   " 

09 

14.0 

99 

37-0 

35h.  23m. 

29  7^3 

89 

3"9 

"   21 

I2.OO   " 

09 

14.0 

99 

41.6 

38h.  ism. 

32253 

141 

3124 

"   22 

3.00  A.M. 

9 

14.0 

99 

55-4 

4ih.  ism. 

34  793 

105 

3128 

"   22 

6.OO   " 

9 

14.0 

99 

53-0 

44h.  I5m. 

37243 

146 

3131 

"   22 

8.30   " 

9 

14.0 

99 

55-4 

4&h.  45m. 

39  293 

67 

3138 

"   22 

12.  OO  M. 

o 

14-5 

102 

4-7 

2h.  4om. 

2  270 

71 

3M3 

"   22 

3.00  P.M. 

o 

14.5 

IO2 

7.0 

5h.  4om. 

4840 

101 

3M9 

"   22 

6.OO   " 

0 

14.0 

99 

7.0 

Sh.  4om. 

739° 

92 

3152 

"   22 

9.OO   " 

o 

14.0 

99 

9-3 

nh.  4om. 

9860 

69 

3156 

"   22 

12.00   " 

o 

14.0 

99 

7.0 

I4h.  4om. 

12  390 

45 

3158 

"   23 

3.00  A.M. 

o 

13-5 

96 

9-3 

I7h.  4om. 

14940 

39 

3161 

'   23 

6.OO   " 

0 

14.0 

99 

13.9 

2oh.  4om. 

17430 

33 

3163 

"   23 

8.30   " 

o 

13-5 

96 

16.2 

23h.  lorn. 

19  420 

34 

3170 

"   23 

12.00  M. 

0 

14.5 

1  02 

16.2 

26h.  4om. 

22330 

72 

3171 

"   23 

3.00  P.M. 

0 

14.0 

99 

18.5 

2gh.  4om. 

24  900 

45 

3176 

"   25 

12.  (.15   " 

o 

14.5 

102 

18.5 

33h.  45m. 

28  260 

91 

3179 

"   25 

2.0O   " 

I) 

14.5 

1  02 

20.8 

35h.  4om. 

29940 

64 

3183 

"   25 

6.OO   " 

0 

14.0 

99 

30.1 

3gh.  40  m. 

32242 

63 

3186 

11  25 

8.00   " 

o 

14.0 

99 

25.5 

4ih.  4om. 

33990 

55 

3190 

."   25 

12.  OO   " 

o 

14.0 

99 

32.4 

45h.  4om. 

38  410 

45 

3193 

"   26 

2.00  A.M. 

o 

14.0 

99 

32.4 

47h.  4om. 

40  090 

33 

3199 

"   26 

6.00   " 

o 

14.0 

99 

39-3 

5ih.  4om. 

43340 

32 

3204 

"   26 

8.30   " 

o 

14.0 

99 

41.6 

54h.  lorn. 

45  3f>o 

369 

3206 

"   26 

9.28   ' 

18.0 

28 

2-3 

nm. 

198 

153 

3207 

"   26 

fg.32   " 

18.0 

28 

2-3 

I5m. 

278 

138 

3210 

"   26 

IO.OO   ' 

17.0 

20 

2-3 

43m. 

758 

138 

3214 

"   26 

2.0O  P.M. 

17.0 

20 

II.  6 

4h.  ,|3m. 

4988 

57 

3217 

"   26 

4.00   " 

17-5 

24 

ii.  6 

6h.  43m. 

7088 

59 

3223 

"   26 

8.00   " 

17-5 

24 

20.8 

loh.  43m. 

II  208 

48 

3226 

"   26 

IO.OO   " 

17-5 

24 

20.8 

I2h.  43m. 

13  308 

68 

323° 

"  27 

2.00  A.M. 

17.0 

2O 

27.8 

i6h.  43m. 

17488 

62 

3232 

I.   27 

4.00   " 

17.5 

24 

30.1 

i8h.  43m. 

19  608 

27 

3238 

"   27 

7.30   " 

'7-5 

24 

32.4 

22h.  I3m. 

23  268 

66 

3244 

"  27 

I2.O5  P-M. 

17.5 

24 

39-3 

26h.  48m. 

27:878 

165 

3247 

"  27 

3.  (JO   " 

17.0 

20 

43-9 

2gh.  43m. 

301818 

36 

3248 

'  27 

3.12   " 

20.  o 

42 

4-7 

0 

o 

900 

Wasting  2  min.,  33  cu.ft. 

3249 

"  27 

3.14   " 

25.0 

77 

4-7 

o 

0 

265 

4  "   63  " 

3250 

..   2? 

3-16   " 

20.0 

42 

4-7 

o 

0 

210 

6  "  103  " 

3251 

"   27 

3.18   " 

15-0 

06 

4-7 

oim. 

17 

igo 

3252 

"  27 

3-22   " 

17.0 

20 

4-7 

osm. 

87 

140 

3253 

"  27 

3.32   " 

18.0 

28 

7-0 

1501. 

267 

119 

3257 

;<  27 

6.00  " 

17-5 

24 

7.0 

2h.  43m. 

2917 

37 

3259 

"  27 

g.(X)  " 

17-5 

24 

9-3 

5h.  43m. 

6027 

32 

3266 

"  27 

12.  00   " 

17-5 

24 

18.5 

8h.  43m. 

9  147 

25 

3268 

"  28 

3-00  A.M. 

17-5 

24 

23-4 

nh.  43m. 

12  227 

30 

3274 

"  28 

6.00  " 

17.0 

20 

30.1 

I4h.  43m. 

15  537 

39 

3277 

"  28 

7.30  " 

2 

I7JJ 

24 

37-0 

i6h.  I3m. 

17077 

"iOO 

COMPOSITION  OF  OHIO  RIVER    WATER   AFTER   PURIFICATION. 
TABLE  No.  4. — Continued. 

Western    Pressure    System. 


I 

kale  of 

j 

u 

Collected. 

Filtr 

at  ion. 

Si 

C 

•£• 

—  

»  i. 

ti. 

Period  of 

"C  * 

,3 

£> 

Number 

S. 

r  ^          _      Service  Si  nee     j;  .=  j 

u  u 

6 

of 

~:  . 

USB,    £    !    Waging. 

•**$. 

G.S 

Remarks. 

S-. 

Date. 

Hour. 

Run. 

ui 

°<o                 Hours  and       -c^  o 
§UI        <           Minuu-s.     |    SS2 

.«! 

•5 

3jg 

5  i  •»      f.                                ~35 

"5 

X 

u 

i        j 

£ 

n 

1896 

3281 

May  28 

0.05  A.M. 

112 

17.0 

120    41.6    iSh.  48111.:  19  897 

74 

3286 

"       28                                 2.14    P.M. 

12 

24.0 

170 

4-7                o 

o 

43°  Wasting  2  min.,   48cu.ft. 

3287 

"       28                                 2.16       " 

12 

20.0 

142      4.7                o 

0 

300        "         4      >'       88      " 

3288 

"28                               2.1$      " 

12 

2O.  O 

42      4.7                o 

o 

282        ••         6      "      108      " 

3289 

"       28                                 2.20       " 

13 

15.0 

(.(>      4.7 

O2m. 

4' 

330 

3290 
3291 

"      28                               2.22       " 
"      28                               2.30      " 

13 

I  " 

15-0 

"" 

4.7              04m. 

7i      235 

3293 

"       28                                  2.00       " 

13 

19.  o 

35   j  4.7       ih.  42m.      i  871      256 

3299 

"       28                                 4.OO      " 

113 

18.0 

28 

9.3      3h.  42m. 

4021       153 

33°7 

"     28                         S.oo     " 

113 

'7-5 

24 

7.0      7h.  4201. 

8091       165 

3313 

11     28 

IO.OO 

113 

18.0 

28 

9.3      gh.  42.11. 

10311       156 

3335 

•;  ;  ;f, 

"     29 

"     29 

2.35  A.M. 
2.  .IS        '' 

114 

16.0 

13 

lorn. 

122 

152 

3341 

"     29                        4.00     " 

"4 

17.0 

20 

9.3      ih.  35m. 

I  652        705 

3344 

'     29 

5-47     ' 

115 

'7-5 

24 

4-7i             05m. 

77      325 

3345 

'     29 

5-57     ' 

H5 

17-5 

24 

4-7              I5m- 

247      4'0 

3357 

'     29 

7.30     " 

1  15 

17-5 

24      4.7       ih.  4801. 

i  847      297 

3362 

'     29 

12.07    I'-M. 

116 

17.0 

20  !   7.0 

5gm. 

9'5 

78 

3365 

"     29 

2.03       " 

116 

15.0 

06  |   7.0 

2h.  55m. 

2  765           69 

3369 

'     29 

6.00     " 

US 

'5-5 

i"      4.7               Igm. 

439      168 

3374 

11     29 

8.00     " 

118 

15-0 

o<) 

4.7      2h.  igm. 

2  269 

34 

3376 

"       2Q 

11.23     " 

119 

2h.  57111. 

2  OI  7 

86 

3379            "     30 

12.24  A.M. 

120 

17.0 

20 

4-7 

28m. 

«  y1  / 

468 

280 

3385 

11       30 

2.29       " 

121 

17-5 

24 

4-7 

iSm. 

298 

369 

3392 

3° 

7.20       " 

I23 

17.0 

1  2O        2.3 

40111. 

658 

118 

3403 

"     30 

12.24    I'-M- 

127 

17.0 

120        7.0 

ogm. 

87 

57 

3407 

June     I 

12.00  M. 

129 

17.0 

120 

7.0 

2h.  54m. 

2933 

67 

34  Io 

"        I 

3.O<>    P.M. 

129 

17.0 

I  2O 

4-7 

5h.  54m. 

5893 

Si 

34M 

"        I 

6.OO       " 

I2g 

17.0 

120 

13.  g      8h.  54m. 

9213 

171 

3416 

I                          g.(x>     " 

132 

20.0 

142 

4.7              04111. 

207 

27 

3421 

"        I 

12.OO       " 

'34 

20.0 

'42 

4-7 

2gm. 

746 

201 

3423 

''          2 

4.OO  A.M. 

136 

'9-5 

138 

2-3 

2301. 

700 

420 

3426 

"          2 

6.45       " 

138 

20.0 

142 

4.7;             16111. 

361 

I87 

3429 

"          2 

10.25       ' 

140 

II.O 

78 

13.9              3om. 

492 

3  gix>  A. 

343" 

"          2 

II.O4 

MI 

16.0 

"3 

2.3 

oim. 

6  1 

68 

3433 

"          2 

12.00  M. 

141 

12.0 

85 

4-7 

57111. 

831 

310 

3437 

"          2 

4.39    P.M. 

143 

12.  O 

85 

2.3 

ih.  i6m. 

i  034 

5  ioo 

A 

344' 

"          2 

6.55     " 

145 

14.0 

99 

4-7 

.     iSm. 

225 

42 

3443 

2 

10  40     " 

148 

14.0 

99 

4-7 

35m. 

561 

41 

3448 

3 

3.30  A.M. 

153 

14.0 

99 

4-7 

04111. 

263 

41 

3452 

3 

6.  20      " 

156 

14.0 

99 

II.  6 

I5m 

237 

54 

34f>9 

3 

6.00  P.M. 

158 

14.0      99 

4-7 

41  m. 

620 

79 

3473 

3 

9.00     " 

'59 

14.0 

99 

4-7 

ih.  48m. 

I  5l8 

73 

3474 

3 

9-37     " 

1  59 

14.0      99 

4-7 

2h.  25m. 

2038 

i  ooo  A. 

3479 

3 

12.  OO      " 

161 

14.0 

99 

4-7 

ogm. 

144 

20 

3483 

4 

3.00  A.M. 

162 

14.1 

99 

Ih.  o6m. 

890 

29 

vt" 

4 

6.OO       " 

162 

14.0      99 

2-3 

4h.  o6m. 

3  260 

184 

349° 

4 

7-05       " 

,63 

14.1 

99 

2-3 

36m. 

456 

29 

3493 

4 

g.OO       " 

164 

J7m 

670 

8 

3497 

4 

10.40       " 

164 

14.0      99 

2-3 

2h.  27rn. 

2059 

'5 

35°° 

4 

1.  10    P.M. 

164 

'3-5 

g6 

4-7 

4h.  57m. 

4079 

87 

3502 

4 

3-4^J       " 

165 

17-5 

24 

2-3 

ih.  46m. 

1875 

23 

3507 

4 

6.28       " 

165 

17.0      20 

2.3 

4h.  28m. 

4685 

97 

35  Io 

4 

8.45       " 

1  66 

17.0        20 

4-7 

ih.  4gm.      I  8og 

19 

3533 

4 

12.  OO       " 

167 

17.0        20 

2-3 

2h.  07m.     2  197 

174 

354° 

5 

3.25  A.M. 

168 

17.0 

20 

2-3 

211.  57m.     2  965 

72 

3544 

5 

6.00     " 

169 

I6.5 

1  6 

2-3 

2h.  i6m.     2  2g4 

32S 

3545 

5 

6.32     " 

169 

I6.5 

16 

2-3 

2h.  48m.     2  714 

I  7«o  A. 

3547 

5 

9.00     " 

171 

JI7.C 

20 

2.3 

46m.  j       647 

21 

3554 

5                       4.05  P.M. 

175 

21.  < 

49 

4-7 

ih.  oom.      i  248 

89 

3555 

5                       4.42     ' 

176 

20.0        42 

2.3 

igm. 

340 

25 

3560 

5 

IO.OO       " 

'77 

20.  C 

42 

4-7 

3h.  i8m. 

3857 

49 

3564 

"       6 

12.30  A.M. 

177 

20.0        42 

4-9 

0 

o 

3'X>  Wasting  3  min.,  7ocu.  ft. 

i84 


WATER   PURIFICATION  AT  LOUISVILLE. 
TABLE  No.  4. — Continued. 

Western    Pressure    System. 


Rs 

teof 

J 

S 

Collected. 

Fill 

ration. 

(I, 

. 

c 

S 

. 

u 

^  i_ 

renoaoi 

V.    ^ 

3  u_- 

1 

a 

Date. 

Hour. 

Number 
Run. 

o. 
fcS 

c  v 

_o  a 

O  0  3 

•a 
£ 

Last 
Washing. 
Hours  and 
Minutes. 

Jlj 

c  «!o 

«  B 

Remarks. 

1 

Is 

^  £»  •* 

0 

r^ 

1" 

3665 

1896 
June    6 

2.23   A.M. 

177 

22.  0 

56 

4-7 

0 

o 

400 

Wasting  6  min.,  135  cu.  ft. 

3566 

"       6 

2-35      " 

178 

2O.  O 

42 

4-7 

02  m. 

31 

37 

3567 

6 

2-37      ' 

178 

20.  0 

42 

4-7 

0(111. 

81 

43 

3568 

"       6 

2-39      " 

178 

18.0 

28 

4-7 

o6m. 

116 

33 

3569 

6 

2.41      ' 

178 

20.  0 

42 

4-7 

o8m. 

156 

5' 

3570 

"       6 

2-43      ' 

178 

2O.  O 

42 

4-7 

lorn. 

196 

22 

3571 

"       6 

2-45     ' 

178 

20.0 

42 

4-7 

I2tn. 

236 

18 

3572 

6 

2-47     ' 

178 

2O.  O 

42 

4-7 

1401. 

276 

51 

3573 

"       6 

2-49     " 

178 

iS.O 

28 

4-7 

i6m. 

311 

37 

3574 

"       6 

2.51      ' 

178 

20.  0 

42 

4-7 

iSm. 

351 

19 

3575 

"       6 

2-53     " 

178 

20.  o 

42 

4-7 

2Om. 

391 

28 

3576 

6 

2-55     " 

178 

20.0 

42 

4-7 

22111. 

43' 

25 

3577 

"       6 

2.57     ' 

178 

2O.  O 

42 

4-7 

24111. 

471 

21 

6 

2.59     " 

178 

21  .0 

49 

4-7 

26m. 

516 

'4 

3579 

"       6 

I  .01       ' 

178 

21  .O 

49 

4-7 

28m. 

561 

67 

358o 

6 

1  .  03     " 

178 

21.  0 

49 

4-7 

30m. 

60  1 

27 

3581 

"       6 

1.  08    " 

178 

20.  0 

42 

4-7 

35m. 

701 

25 

3582 

"       6 

1.18     " 

178 

2O.  O 

42 

4-7 

45"i. 

911 

39 

3583 

6 

1-33     " 

178 

20.0 

42 

4-7 

ill.  oom. 

I  211 

47 

6 

1  .43     " 

178 

ih.  lom. 

I  426 

800 

A. 

3587 

6 

2-33     '' 

179 

20.0 

42 

2-3 

35m. 

665 

26 

3597 

6 

'79 

2O.  O 

42 

4-7 

5h.  53m. 

68l5 

3625 

6 

10.58     " 

179 

20.0 

42 

4-7 

5h.  4om. 

850 

31 

3630 

6 

1.55    P.M. 

183 

2O.  0 

42 

2-3 

o6m. 

273 

69 

3633 

6 

3-04      " 

183 

19.5 

38 

4-7 

ih.  1501. 

I  503 

31 

9 

1.30      " 

1  86 

20.0 

42 

2-3 

igm. 

375 

121 

3670 

'     10 

I  I.  2O    A.M. 

189 

17-5 

24 

4-7 

2h.  1401. 

I  374 

29 

3673 

"       10 

I  .00    P  M. 

189 

18.0 

28 

4-7 

3h.  54m. 

4184 

104 

3677 

"     10 

3.30       " 

191 

'7-5 

24 

2.3 

38m. 

806 

2g 

3683 

"     ii 

10.40    A.M. 

193 

18.0 

28 

2.3 

ih.  ism. 

14^3 

9 

3686 

"     ii 

I.  2O     P.M. 

194 

17-5 

24 

4-7 

I2m. 

198 

19 

3694 

"     1  1 

3-45     " 

195 

17.0 

20 

2-3 

iqm. 

366 

4 

3698 

"       12 

IO.2O    A.M. 

195 

18.0 

28 

2-3 

3)1.  24111. 

3  596 

12 

3705 

"       12 

2.42     P.M. 

196 

17-5 

24 

4-7 

35tn. 

631 

17 

3712 

"       "3 

IO.  14    A  M. 

197 

20.  o 

42 

4-7 

ih.  urn. 

I  470 

16 

3720 

'     13 

1.25     P.M. 

198 

2O.  0 

42 

2-3 

2401. 

5O1 

17 

3726 

'     J3 

2.57       " 

198 

20.  o 

42 

7-0 

ih.  5&m. 

2311 

320 

3729 

'      13 

5.03       " 

199 

18.0 

28 

2.3 

ih.  43m. 

I  858 

18 

"      '5 

g.OO   A.M. 

199 

118 

B. 

3742 

"      15 

IO.I8       " 

199 

18.0 

28 

2-3 

3h.  28m. 

3778 

23 

3745 

'      15 

12.25     f.M. 

199 

17.5 

24 

7.0 

5h.  35m. 

6  108 

16 

3749 

"     15 

3-05       " 

2CO 

18.0 

28 

4-7 

som. 

933 

41 

3755 

'     '5 

4-33       " 

2O  I 

17.0 

20 

2-3 

43m. 

790 

27 

3761 

"     16 

IO.29    A.M. 

201 

18.0 

28 

4-7 

3h.  09111. 

3  330 

16 

37^5 

"      16 

12.40    P.M. 

2O  [ 

18.0 

28 

4-7 

5h.  2om. 

5  600 

52 

3768 

"      16 

3.29       " 

202 

18.0 

28 

2-3 

2h.  09111. 

2387 

46 

3773 

"     16 

4-32       " 

203 

.8.5 

32 

2-3 

27m. 

482 

17 

3777 

"      17 

IO.O8    A.M. 

203 

18.5 

32 

4-7 

2h.  33111. 

2882 

24 

3779 

'      17 

12.52       " 

203 

18.0 

28 

4-7 

5h.  I7m. 

5  792 

21 

3784 

'     17 

2.55   P.M. 

2O4 

17.5 

24 

2-3 

56m. 

i  in 

37 

3792 

'     17 

4.22       " 

204 

18.0 

28 

2-3 

2h.  23m. 

2  701 

37 

379s 

"     18 

IO.  12    A.M. 

205 

18.0 

28 

4-7 

ih.  05111. 

I  273 

212 

3803 

"     18 

12.37    P.M. 

205 

18.0 

28 

4-7 

3(1.  3om. 

3923 

I03 

3811 

"     18 

2.52       " 

205 

18.0 

28 

4-7 

5h.  45m. 

6303 

169 

3820 

"     '9 

IO.O4    A.M. 

2O6 

iS.o 

28 

4-7 

58111. 

I  129 

26 

3831 

'     19 

3.07     P.M. 

208 

18.0 

28 

4-7 

42m. 

702 

53 

•jg  17 

"      19 

4.25       " 

208 

2h.  oom. 

2  l6l 

1  1 

JU4  / 
3857 

"       20 

II.lS    A.M. 

20g 

18.0 

28 

2-3 

2h.  I2m. 

2341 

103 

3864 

"       20 

12.46    P.M. 

2O9 

18.0 

28 

4-7 

3h.  4001. 

3941 

43 

3871 

"       20 

3-25      " 

210 

18.0 

28 

2-3 

ih.  36m. 

I  683 

54 

3876 

"       2O 

4.40      " 

211 

18.0 

28 

2.3 

o6m. 

103 

93 

3885 

"       22 

10.22    A.M. 

211 

18.5 

32 

2h.  1401. 

2503 

41 

3890 

"      22 

1.23    P.M. 

211 

18.5 

32 

5h.  igm. 

5  923 

91 

COMPOSITION  OF  OHIO   RIVER    WATER  AFTER   PURIFICATION.  185 


TABLE  No.  4. — Continued. 

Western     Pressure    System. 


Rale  of 

J 

- 

Collected. 

Fi  tration. 

£ 

J 

•£ 

Jj 

Number 

1 

JS. 

•o 

Period  of 
ServiceSinc 

.  bi 
*•-  - 

o  u. 

e 

Date. 

Hour. 

Run. 

(L.S 

fli 

X 

Washing. 
Minutes! 

||| 

ks 

Remarks. 

% 

u 

A 

2 

£ 

ta 

1896 

38g6 

June  23 

2.22  P.M. 

211 

6h.  iSm 

7  044    3 

3956 

"   24 

3.26   " 

212 

20. 

125 

2.3 

ih.  36m 

I  gig   iSf 

3966 

24 

4-54  " 

212 

20.0 

142 

3h.  04171 

36g? 

250 

3g85 

25 

IO.  l6  A.M. 

212 

18.0 

128 

4-7 

4h.  56m. 

5949 

36c 

4003 

1   25 

1.18  P.M. 

212 

2O.  c 

142 

7-o 

7h.  58m. 

9469 

35 

4004 

"   25 

1-54  '* 

212 

4007 

"   25 

3-i8  " 

213 

,  '  •• 

i  300  i  oot)' 

4014 

"   25 

5.00  " 

214 

18.0 

128 

4-7 

ih.  igm 

i  354i   63 

4025 

"   26 

10.29  A.M. 

214 

iS.o 

128 

4-7 

3h.  iSm 

3444    12 

4032 

"   26 

I.I7  P.M. 

214 

iS.o 

128 

7.0 

6h.  o6m 

6  3«4   42 

4033 

"   26 

1.22   " 

214 

6h.  1  1  m 

6481 

cn 

4036 

"   26 

3-30   " 

215 

18.0 

128 

4-7 

ih.  3im 

1643 

JV 

Si 

4038 

"   26 

4-54  ' 

2|6 

18.0 

128 

4-7 

I2rn 

I74l   59 

4045 

"   27 

IO.3O  A.M. 

216 

18.0 

128 

2-3 

2h.  i6m 

2434 

127 

4051 

1   27 

1.  00  P.M. 

2l6 

18.0 

128 

4h.  4601 

5058 

4053 

:   27 

2.03   " 

217 

18.0 

128 

2-3 

42m 

4054 

1   27 

3-15   " 

218 

18.0 

128 

ogm 

157 

370 

4057 

27 

4-51  ' 

218 

iS.o 

128 

2-3 

ih.  45m 

1*57  

4063 

1   29 

IO.I8  A.M. 

219 

18.0 

128 

2-3 

ih.  nm 

i  327 

12 

4065 

1   29 

12.30  P.M. 

220 

18.0 

128 

7.0 

ogm 

156 

29 

4069 

29 

1.32   " 

220 

i.S  .1 

128 

2.3 

ih.  inn 

I  306 

63 

4071 

29 

3-40  " 

221 

18.0 

128 

2-3 

30111 

529 

4083 

1   30 

IO.I6  A.M. 

222 

18.0 

128 

4-7 

ih.  0701. 

I  220 

32 

4101 

'   30 

12.47  I'-M. 

223 

18.0 

128 

4-7 

22rn 

356 

34 

4106 

30 

2.55  " 

224 

18.0 

128 

4-7 

24111 

sgs 

32 

4U5 

July   I 

IO.27  A.M. 

225 

18.0 

128 

4-7 

ih.  2701. 

1464 

4124 

I 

i.ig  P.M. 

2-26 

18.5 

132 

2.3 

35m. 

630  

4132 

"    I 

3-19  " 

227 

17-5 

124 

2-3 

48m. 

830  

4136 

"    I 

4-37  ' 

228 

18.0 

128 

2.3 

38m. 

655  

4206     "    6 

10.30  A.M. 

229 

17.0 

1  20 

7.0 

ih.  i8m. 

i  284   13 

4211 

6 

12.43  P.M. 

22g  . 

17.0 

1  20 

7-o 

3h.  3im. 

3  574 

24 

4239 

6 

5-19   " 

22g 

17-5 

124 

4-7 

8h.  07111. 

8334 

108 

4247 

7 

IO.OO  A.M. 

230 

21.5 

152 

7.0 

49111. 

i  265 

22 

4254 

7 

1.  00  P.M. 

231 

19.  o 

7-0 

25m. 

868 

49 

4256 

7 

3.00   " 

232 

18.0 

128 

23111. 

567 

19 

4265 

8 

10.55  A.M. 

233 

iS.o 

128 

4-7 

ih.  4801. 

2  184 

II 

4268 

8 

12.45  P.M. 

233 

18.0 

128 

3h.  38m. 

3984 

33 

4272 

8 

3-54   ' 

234 

2h.  oom. 

i  868 

20 

4281 

9 

10.30  A.M. 

235 

17.0 

1  20 

4-7 

ih.  25m. 

i  375 

6 

4284 

9 

12.28  P.M. 

235 

17.0 

1  20 

9-3 

3h.  23m. 

3345 

10 

4303 

g 

3-27   " 

i  h  .  5  1  in  . 

i  885 

112 

4310 

9 

5-13   " 

237 

16.5 

116 

7.0 

ih.  13m. 

i  205 

112 

4368 

13 

IO.  19   " 

238 

17.0 

1  20 

7.0 

ih.  oSm. 

1074 

25 

4372 

13 

12.00   " 

238 

17.0 

120 

4-7 

2h.  4gm. 

2784 

98 

4374 

13 

3-05   " 

23g 

17.0 

1  20 

4-7 

ogm. 

120 

no 

4380 

M 

g.o4  A.M. 

239 

II.  0 

78 

o 

O 

249 

Wasting  4min.,  55  cu.  ft. 

i  i-  1 

14 

9.07  " 

239 

ii..  1  1 

"3 

o 

O 

446 

Wasting  7  min.,  78  cu.  ft. 

4382 

'4 

9.12  ' 

240 

16.5 

116 

2-3 

osm. 

82 

1  86 

43*3 

M 

9-17  " 

240 

16.5 

116 

2-3 

lorn. 

'72 

71 

43*4 

14 

9.22  " 

240 

16.5 

116 

2-3 

15111. 

262 

59 

4385 

14 

9-27  " 

240 

16.5 

116 

2-3 

2om. 

342 

32 

4387 

M 

9-32  ' 

240 

17.0 

120 

2-3 

25m. 

442 

45 

4389 

14 

9-37  ' 

240 

'7-5 

124 

2.3 

3om. 

532 

37 

439° 

'4 

9-42  " 

240 

17-5 

124 

2.3 

35m. 

622 

33 

4391 

14 

9-47  ' 

240 

17-5 

124 

2-3 

40111. 

702 

14 

4392 

M 

9-52  ' 

240 

17.0 

120 

2.3 

45111. 

782     13 

4393 

14 

9-57  ' 

240 

17-5 

124 

2.3 

5om. 

872    15 

4394 

14 

O.O2   " 

240 

'7-5 

124 

2-3 

55m. 

952    7 

4395 

M 

0.07   " 

240 

17.0 

1  2O 

2-3 

ih.  oom. 

i  032   13 

I  jip 

14 

O.22   " 

240 

[7.0 

120 

2.3 

ih.  15m 

i  282!    5 

4399 

14 

0.37   " 

240 

17.0 

1  2O 

2-3 

ih.  3om. 

I  532     2 

4400 

M 

0.52   " 

240 

[7.0 

120 

2-3 

ih.  45m. 

i  782;    7 

4401 

14 

1.07   ' 

-  1" 

1  '.-i  . 

2.  ; 

2ll.  1X)T1). 

2  032'  108 

i86 


WATER   PURIFICATION  AT  LOUISVILLE. 
TABLE  No.  4. — Concluded. 

Western    Pressure    System. 


Ra 

r  -1 

-; 

o 

:ollected. 

Filtr 

uion. 

1 

S  . 

15 

- 

V 

,-.    '" 

Period  of 

u  £? 

3 

u 

Number 

o. 

0   & 

•o 

ServiceSince 

i;  •-  ^j 

CJ  ^* 

1 

55 

Run. 

fe  ~ 

5li' 

» 

Last 
Washing 
Hours  and 

£|fc 
•at*  u 

c 

Remarks. 

Date. 

Hour. 

p 

If 

^ 

Minutes. 

Ssl 

§1 

'C 

la 

o 

-JU 

«<-> 

c/i 

u 

ia" 

J 

(i. 

CO 

1896 

4402 

July  14 

11.22  A.M. 

240 

17.0 

1  20 

2.3 

2h.  I5m. 

2  292 

4 

4403 

'      14 

"•37     " 

240 

17.0 

1  20 

4-7 

2h.  3om. 

2  502 

8 

4404 

'      M 

11.52     " 

240 

17.0 

1  20 

4-7 

2h.  45m. 

2  802 

2 

4405 

'      M 

12.07  P.M. 

240' 

17.0 

120 

4-7 

3h.  oom. 

3042 

7 

4406 

'      M 

12.22       " 

240 

17.0 

I2O 

7.0 

3h.  1501. 

3292 

9 

4407 

'      14 

12.37       " 

240 

17.0 

120 

9-3 

3h.  3om. 

3542 

2 

4408 

'     14 

12.52       ' 

240 

16.5 

116 

9-3 

3h.  45m. 

3792 

3 

4413 

'      M 

1.07       ' 

240 

16.5 

116 

9-3 

4h.  oom. 

4042 

I 

4414 

'      M 

1.22       " 

240 

17.0 

1  20 

7.0 

4h.  ism. 

4302 

II 

4415 

'      M 

1-37       " 

240 

17.0 

1  20 

7.0 

4h.  3om. 

4502 

4 

4416 

'      M 

1.52       " 

240 

17.0 

1  20 

9-3 

4h.  45m. 

4812 

0 

4417 

'      M 

2.07       ' 

240 

17- 

1  20 

9-3 

5h.  oom. 

5072 

I 

4418 

'      14 

2.22       " 

240 

17- 

1  20 

9-3 

5h.  I5m. 

5322 

0 

4419 

'      M 

2.37       " 

240 

17. 

1  20 

u.  6 

5h.  30111. 

5  572 

10 

4420 

'      M 

2.52       " 

240 

17- 

120 

9-3 

5h.  45m. 

5  822 

ii 

4421 

'      M 

3.07       " 

240 

17. 

1  2O 

6h.  oom. 

6082 

54 

4445 

'      15 

2.19       " 

241 

16. 

"3 

7-0 

ih.  o8m. 

i  070 

7 

445<> 

'      15 

3-19       " 

241 

16. 

116 

7.0 

2h.  o8m. 

2  ogO 

u 

4451 

'      15 

4-49       " 

241 

17- 

120 

7.0 

3h.  3Sm. 

3  OoO 

15 

4458 

"      16 

9.47  A.M. 

242 

17- 

120 

4-7 

39m. 

680 

18 

4461 

"      if 

II.08       ' 

242 

17. 

I24 

7.0 

2h.  oom. 

2  080 

0 

4471 

"      if 

I.l6  P.M. 

243 

17- 

I  2O 

4.6 

22m. 

380 

31 

4572 

"       2( 

II.  21  A.M. 

245 

17- 

I  2O 

7.0 

2h.  I7m. 

2307 

lO 

4574 

"      20 

1.37    P.M. 

245 

17- 

120 

5-9 

4h.  33m. 

4607 

31 

4577 

"       20 

3-31       ' 

245 

17- 

120 

9-3 

Oh.  27m. 

f'5i7 

20 

4579 

"       2( 

5.06      " 

245 

17- 

I  2O 

9-3 

8h.  02m. 

8  117 

23 

4585 

"       2 

9.05  A.M. 

245 

14. 

99 

9-3 

o 

o 

820 

Wasting  5  min.,  78  cu.  ft. 

458f 

"       2 

9.10      " 

246 

17- 

120 

9-3 

osm. 

05 

192 

4587 

"       2 

9-15       ' 

246 

17- 

120 

13-9 

zom. 

145 

82 

4588 

"       2 

9.20      " 

246 

17- 

1  2O 

7.0 

I5m. 

235 

72 

4589 

"       2 

9.25       " 

246 

17- 

120 

7.0 

2om. 

315 

41 

4590 

"       2 

9.30      " 

246 

17- 

120 

7.0 

25111. 

405 

32 

4592 

"       2 

9-35     ' 

246 

17.0 

1  2O 

7.0 

3om. 

485 

190 

4593 

"       2 

9.40     " 

246 

16.5 

116 

7.0 

35m. 

575 

207 

4594 

"       2 

9-45     ' 

246 

16.5 

116 

7-0 

40111. 

045 

193 

4595 

"       2 

9.50     " 

246 

16.5 

116 

7-o 

45m. 

735 

171 

4596 

"       2 

9-55     ' 

246 

16.5 

116 

7-o 

5om 

815 

225 

4597 

"       2 

IO.OO       " 

246 

,6.5 

116 

4-7 

55m 

895 

lOg 

4598 

"       2 

10.15    " 

246 

iS.o 

128 

7-o 

ih.  lom 

i  155 

195 

4599 

"       2 

10.30   " 

246 

18.0 

128 

7.0 

ih.  25m 

i  425 

203 

4600 

"       2 

10.45    ' 

246 

18.0 

128 

9-3 

ih.  4om. 

1085 

133 

4601 

"       2 

II.  OO       " 

246 

18.0 

128 

7-o 

ih.  55m 

i  965 

154 

460^ 

"       2 

11.02       " 

246 

18.0 

128 

7-o 

ih.  57m. 

I  995 

137 

4&<x 

"       2 

11.30       " 

246 

18.0 

128 

4-7 

2h.  25m 

2485 

509 

4605 

"       2 

12.  OO       " 

246 

18.0 

128 

4-7 

2h.  55m 

3035 

498 

4607 

"       2 

I2.3O  P.M. 

246 

18.0 

128 

7.0 

3h.  25m 

3  555 

299 

4610 

"       2 

1.26       " 

247 

17.0 

1  20 

4-7 

23m 

370 

357 

4611 

"       2 

3-05       " 

248 

16.0 

"3 

7.0 

I5m 

227 

292 

461^ 

"       2 

5.05       " 

248 

16.0 

"3 

7.0 

2h.  ism 

2077 

158 

4621 

"       2 

11.14  A-M. 

249 

15-5 

no 

7-o 

2h.  ogm 

2  OOI 

040 

4626 

"       2 

2.44  P.M. 

251 

14-5 

1  02 

7.0 

4601 

072 

37 

4630 

"       2 

4-03       " 

251 

14.0 

99 

16.2 

2h.  O5m. 

I  792 

i  186 

4729 

"       27 

11.58  A.M. 

254 

14.5 

IO2 

7.0 

44m 

&44 

145 

473° 

'       27 

1.56  P.M. 

254 

14.0 

99 

i  1.1 

2h.  32m 

2364 

170 

4734 

"       27 

3.IO       " 

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SUMMARY  AND   DISCUSSJOiV   OF  DATA    OF   1895-96. 


CHAPTER   IX. 

SUMMARY  OF  THE  PRINCIPAL  DATA  UPON  THE  EFFICIENCY  AND  ELEMENTS  OF  COST 
OF  PURIFICATION,  BY  THE  RESPECTIVE  SYSTEMS,  OF  THE  OHIO  RIVER  WATER,  DI 
VIDED  INTO  TWENTY  PERIODS,  ACCORDING  TO  THE  CHARACTER  OF  THE  UNPURIFIED 
WATER  ;  TOGETHER  WITH  A  DISCUSSION  OF  SOME  OF  THE  MORE  IMPORTANT 
FEATURES. 


BEFORE  the  presentation  of  a  summary  of 
the  principal  data  obtained  during  1895-6 
upon  the  efficiency  and  the  elements  of 
cost  of  the  purification  of  the  Ohio  River 
water,  in  twenty  periods,  according  to 
the  character  of  the  unpurified  water,  there 
will  be  given  as  a  matter  of  record  some  tabu 
lations  showing  the  character  of  the  purified 
water  by  days.  For  a  detailed  account  of  the 
composition  of  the  Ohio  River  water  by  days, 
and  of  the  amount  of  sulphate  of  alumina  ap 
plied  to  the  river  water,  reference  is  made  to 
Chapters  I  and  II,  respectively.  The  ques 
tion  of  the  decomposition  of  the  sulphate  of 
alumina  and  its  removal  from  the  water  was 
discussed  carefully  in  Chapter  III. 

Table  No.  i. 

The  first  set  of>  tables  in  this  chapter  con 
tains  a  daily  statement  of  the  appearance  of 
the  water  after  purification  by  the  respective 
systems.  As  already  explained  the  appear 
ance  of  the  filtered  water  is  designated  by  five 
degrees  of  clearness,  which  may  be  described 
briefly  as  follows: 

Degree  No.  i  signifies  a  brilliant  water. 

Degree  No.  2  signifies  a  clear  water. 

Degree  No.  3  signifies  a  slightly  turbid 
water. 

Degree  No.  4  signifies  a  turbid  water. 

Degree  No.  5  signifies  a  very  turbid  water. 

The  first  three  degrees  of  clearness  refer  in 
each  case  to  an  appearance  of  the  water 
which  is  satisfactory.  It  is  doubtful  if  the  con 
sumers  would  distinguish  between  these  three 
degrees  of  clearness  unless  their  attention 


were  directed  to  the  matter.  Degrees  Nos.  4 
and  5  would  be  noted  by  the  consumers,  but 
it  is  to  be  stated  that  the  adjectives  used 
above  have  only  a  comparative  value  in  rela 
tion  to  a  brilliant  water. 

In  both  cases  the  turbiditv  would  be  very 
slight  when  compared  with  the  river  water 
before  purification. 

Degree  No.  4  refers  to  an  appearance 
which  would  not  be  unsatisfactory  for  short 
periods  if  the  water  were  of  a  proper  charac 
ter  in  all  other  particulars.  Degree  No.  5 
was  objectionable  both  in  its  direct  and  in 
direct  bearings,  and  was  seldom  noted  for 
periods  of  long  duration. 


In  the  second  set  of  tables  arc  recorded  the 
percentages  of  removal  from  the  river  water, 
by  the  respective  systems,  of  the  carbon 
aceous  and  nitrogenous  organic  matter,  as 
indicated  by  the  oxygen  consumed  and  the 
nitrogen  in  the  form  of  albuminoid  ammonia, 
respectively.  As  a  matter  of  convenience  the 
total  amount  of  nitrogen  in  the  form  of  al 
buminoid  ammonia  in  the  river  water,  and 
the  percentage  of  the  total  amount  which  was 
found  to  be  undissolved  in  the  water,  are 
given.  It  will  be  obsereved  that  the  total 
amount  of  nitrogeneous  organic  matter  in 
the  filtered  water  was  less  than  the  amount 
dissolved  in  the  river  water  before  purification. 

Table  No.  .?. 

The  third  set  of  tables  contains  a  record  of 
the  daily  average  number  of  bacteria  per  cubic 


2l6 


WATER   PURIFICATION  AT  LOUISVILLE. 


centimeter  in  the  Ohio  River  water  before 
and  after  purification  by  the  respective  sys 
tems,  and  also  the  daily  average  bacterial 
efficiency  of  each  system.  Bacterial  efficiency 
means  the  percentage  which  the  difference  in 
the  numbers  of  bacteria  in  the  water  before 
and  after  purification  is  of  the  number  of  bac 
teria  originally  present  in  the  river  water. 


In  the  next  set  of  tables  are  presented  the 
principal  data  obtained  during  the  investiga 
tions  with  regard  to  the  efficiency  and  cost  of 
purification  by  this  method.  As  stated  at  the 
outset  of  this  chapter  the  results  are  divided 
into  twenty  periods,  according  to  the  charac 
ter  of  the  unpurified  river  water.  This  was 
necessitated  by  the  marked  variations  in  the 
composition  of  the  river  water,  affecting  both 
the  efficiency  and  the  cost  of  purification;  and 
also  by  the  varying  conditions  under  which 
the  respective  systems  were  operated. 

The  official  investigations  of  the  several 
systems  of  purification  by  the  method  in  ques 
tion  began  on  Oct.  21,  1895.  For  a  number 
of  weeks  after  that  time  the  investigations 
were  less  exhaustive  than  they  were  during 
the  later  portion  of  the  period  when  the 
laboratory  work  had  been  more  fully  planned 
to  meet  the  requirements  of  the  problem. 
The  Warren  System  began  operations  during 
the  latter  half  of  September.  On  October  21 
the  operators  of  this  system  contemplated 
some  modifications  in  its  construction.  Ow 
ing  to  the  remarkably  low  stage  of  the  river 
at  that  time  it  was  desirable  for  the  Water 
Company  to  obtain  data  with  this  character 
of  water. 

Accordingly  they  were  officially  requested 
to  postpone  their  changes  for  a  short  time  and 
operate  the  system  with  varied  amounts  of 
sulphate  of  alumina  from  day  to  day.  This 
the}'  consented  to  do,  but  protested  against 
the  merits  of  their  system  being  judged  from 
operations  preceding  their  contemplated 
changes. 

Operation  of  the  Jewell  System  began 
early  in  July,  1895,  and  was  said  to  have  been 
continued  nearly  every  day  up  to  October  21, 
the  commencement  of  the  official  tests. 

The  installation   of  the   Western   Systems 


did  not  begin  until  early  in  November,  and  it 
was  not  until  December  23  that  they  were 
ready  for  regular  official  inspection.  Explana 
tion  has  already  been  given  of  the  lengthy 
delays  in  these  systems  after  about  April  i. 
From  March  24  to  30  and  April  27  to  June 
6  all  systems  were  requested  by  the  Water 
Company  to  be  operated  twenty-four  hours 
per  day,  excepting  Sundays  during  the  latter 
period.  Otherwise  the  systems  were  operated 
about  8.5  hours  per  day  (irom  9  A.M.  until 
5.30  P.M.). 

A  brief  account  is  next  given  of  the  several 
periods  into  which  the  investigations  are  di 
vided  according  to  the  grade  of  the  river 
water  and  other  conditions  of  operation. 


Period  No.  i. — This  period  extended  from 
Oct.  21  to  Xov.  25,  1895.  It  represents  the 
last  portion  of  the  most  severe  and  extended 
drought  which  had  been  noted  for  many 
years.  With  the  low  stage  of  the  river  there 
was  an  absence,  comparatively  speaking,  of 
suspended  organic  and  mineral  matters  in  the 
river  water;  the  amounts  of  dissolved  organic 
and  mineral  matter  were  abnormally  high; 
and  the  bacteria,  while  comparatively  few  in 
number,  contained  an  unusually  large  propor 
tion  of  species  coming  from  the  sewage  of 
cities  situated  farther  up  in  the  valley. 

The  Jewell  System  was  the  only  one  that 
was  in  service  during  the  full  period.  The 
Warren  System  was  in  service  for  a  consider 
able  portion  of  the  time,  but  under  the  con 
ditions  stated  above;  while  the  installation  of 
the  Western  Systems  was  not  completed. 

Period  No.  2. — This  period  extended  from 
Nov.  25  to  Dec.  24.  During  this  time  light 
rains  fell.  The  water  varied  somewhat  in 
character.  At  times  the  indications  of  sewage 
pollution  were  more  marked  than  during  the 
first  period.  The  water  became  more  muddy, 
and  the  chlorine  and  alkalinity  decreased  in 
a  marked  degree  toward  the  end,  although 
this  did  not  follow  in  the  case  of  the  other 
soluble  constituents.  In  fact  there  was  an 
increase  in  some  of  them,  notably  in  the  ni 
trogen  as  free  ammonia.  With  the  rains  the 
number  of  bacteria  increased  considerably. 

The  Warren  and  Jewell   systems  were  in 


SUMMARY  AND   DISCUSSION  OF  DATA    OF   1895-96. 


217 


regular  service  during  this  period,  hut  the 
Western  Systems  did  not  begin  operation  un 
til  it  was  practically  ended. 

Period  No.  j. — This  period  extended  from 
Dec.  24,  1895,  to  Jan.  13,  1896.  It  repre 
sents  the  rising,  maximum  and  falling  stage 
of  the  river  after  the  first  heavy  storm  of  the 
season.  From  this  time  to  the  close  of  the 
tests  the  chief  variation  in  the  river  water  was 
the  amount  of  suspended  matter  which  it  con 
tained.  These  amounts  will  he  noted  in  the 
tables. 

All  four  systems  were  in  service. 

Period  No.  4. — This  period  extended  from 
Jan.  13  to  27,  1896.  It  represents  a  fairly 
uniform  grade  of  the  river  water  from  the  fall 
of  the  preceding  rise  to  the  beginning  of  the 
next  subsequent  one. 

All  four  systems  were  in  service  during  the 
greater  part  of  the  time.  The  sand  layer  of 
the  Warren  System  was  changed  on  Jan.  23. 

Period  No.  5. — This  period  extended  from 
Jan.  27  to  Feb.  6,  and  represents  a  rising 
stage  of  the  river  and  increasing  amounts  of 
suspended  matter  in  the  river  water. 

For  unavoidable  reasons  the  Western 
Systems  were  out  of  service  on  Jan.  29  and 

3°- 

On  Feb.  i  the  scope  of  the  investigations 
was  enlarged.  The  sand  layer  of  the  Jewell 
System  was  changed  on  this  date. 

Period  No.  6. — This  period  extended  from 
Feb.  6  to  13,  and  represents  the  height  of  a 
rise  in  the  river  when  of  course  the  suspended 
matter  in  the  water  was  unusually  high  in 
amount. 

From  Feb.  8  until  about  April  i  lime  was 
applied  to  the  river  water  in  the  case  of  the 
Jewell  System. 

All  four  systems  were  in  service,  but  the 
Warren  System  was  delayed  from  time  to 
time  by  changes  in  the  devices  for  the  intro 
duction  of  wash-water  beneath  the  sand  layer. 

Period  No.  J. — This  period  extended  from 
Feb.  13  to  27.  and  represents  a  falling  stage 
of  the  river  with  decreasing  amounts  of  sus 
pended  matter  in  the  river  water. 

The  most  noteworthy  features  in  the  op 
eration  of  the  several  systems,  speaking  in 
general  terms,  were  the  irregular  results 
along  several  lines,  particularly  those  of  bac 
terial  efficiency  and  application  of  chemicals. 


Period  No.  8. — This  period  extended  from 
Feb.  27  to  March  20,  and  represents  com 
paratively  clear  water  between  successive  rises. 
All  of  the  systems  were  quite  regularly  in 
service.  On  March  16  the  operators  of  the 
respective  systems  were  officially  asked  to 
comply  with  certain  requests,  leading  to  more 
regular  and  more  efficient  results  of  purifica 
tion.  On  Feb.  29  a  new  and  separate  pipe 
for  the  supply  of  river  water  was  connected 
with  the  Western  Systems. 

Period  No.  9. — This  period  included  March 
20  and  21,  and  represents  very  muddy  water 
at  the  beginning  of  an  extended  freshet. 

The  Western  Gravity  System  went  out  of 
service  owing  to  its  failure  to  purify  enough 
water  to  serve  for  washing  its  own  sand 
layer.  ; 

Period  No.  10. — This  period  extended  from 
March  23  to  30,  and  represents  a  muddy  con 
dition  of  the  water  and  a  high  stage  of  the 
river.  The  suspended  matter  for  the  most 
part  had  a  red  color,  however,  and  was  much 
coarser  than  was  noted  under  other  condi 
tions. 

From  March  24,  9.00  A.M.,  to  March  30, 
5.30  P.M.,  the  systems  were  operated  con 
tinuously,  with  the  exception  of  the  Western 
Gravity  System,  which  was  not  operated  at  all. 

Period  No.  //.—This  period  extended  from 
March  30  to  April  7,  and  represents  a  muddy 
water  and  falling  stage  of  the  river.  Rains 
caused  the  water  to  vary  considerably  in  char 
acter. 

All  systems  except  the  Western  Gravity 
System  were  in  service. 

On  April  3  the  representatives  of  the  re 
spective  systems  were  officially  requested  to 
get  in  readiness  to  operate,  upon  48  hours' 
notice,  their  systems  night  and  day  for  such 
periods  as  the  Water  Company  deemed  ad 
visable. 

Period  No.  12. — This  period  extended  from 
April  7  to  27,  and  represents  a  falling  stage  of 
the  river  and  comparatively  clear  water.  The 
end  of  this  period  marked  Ihe  beginning  of 
a  six  wrecks'  period  of  continuous  operation 
during  each  week  from  9.00  A.M.  on  Monday 
to  4  P.M.  on  Saturday. 

This  period  was  chiefly  characterized  by  re 
pairs,  following  the  official  communications 
of  March  16  and  April  3,  as  noted  above. 


2l8 


WATER   PURIFICATION  AT  LOUISVILLE. 


In  the  Warren  System  the  sand  layer  was 
changed.  This  caused  a  delay  from  April  13 
to  20.  The  Jewell  System  was  in  regular  ser 
vice.  Neither  of  the  Western  Systems  was 
operated  at  all  during  this  period. 

Period  Arc>.  /j. — This  period  extended  from 
April  27  to  May  18,  and  represents  a  period 
of  comparatively  clear  water  in  the  middle  of 
a  protracted  drought.  It  also  represents  the 
first  half  of  the  six  weeks'  period  of  continu 
ous  operation. 

The  Warren  and  Jewell  systems  were  regu 
larly  in  service.  From  May  7  until  the  close 
of  the  period  the  Western  Pressure  System  was 
in  regular  operation.  At  about  the  same  date 
the  repairs  of  the  Western  Gravity  System 
were  also  completed.  It  was  operated  un 
officially  on  several  occasions,  but  it  was  not 
put  in  official  operation  until  after  the  Water 
Company  requested  an  official  explanation  of 
the  reason  of  its  withdrawal  from  the  tests. 
This  request  was  made  during  the  last  week 
in  June.  During  the  intervening  period  this 
system  was  left  out  of  consideration  by  all 
parties  so  far  as  active  operations  were  con 
cerned. 

Period  No.  /-/. — This  period  extended  from 
May- 18  to  28,  during  the  time  of  continuous 
operation,  and  represented  the  last  portion  of 
the  comparatively  clear  water,  before  the  end 
of  the  long  drought.  During  this  period  the 
conditions  of  operation,  with  regard  to  rate 
of  filtration  and  amount  of  applied  sulphate  of 
alumina,  were  prescribed  by  the  Water  Com 
pany  as  shown  in  table  No.  4  of  the  last  chap 
ter. 

No  unusual  delays  occurred  in  the  case  of 
the  Warren,  Jewell,  and  Western  Pressure 
systems,  except  as  occasioned  by  the  pre 
scribed  conditions. 

Period  Aro.  75. — This  period  extended  from 
May  28  to  June  3,  and  represents  a  rapidly 
rising  stage  of  river  when  the  suspended  mat 
ter  was  in  part  exceedingly  fine,  as  noted  in 
Chapter  T. 

Great  difficulty  in  securing  coagula 
tion,  even  with  large  amounts  of  sulphate  of 
alumina,  was  experienced..  Conditions  of 
continuous  operations,  as  above  outlined, 
were  prescribed  by  the  Water  Company  so 
far  as  it  was  practicable. 

Period  ATo.  16. — This  period  extended  from 


June  3  to  9,  and  represents  the  last  of  the  con 
tinuous  operations  for  24  hours  per  day;  and 
also  the  last  of  the  prescribed  conditions. 
The  water  was  muddy  but  rather  variable  in 
character. 

The  Warren,  Jewell,  and  Western  Pressure 
systems  were  in  operation  without  any  seri 
ous  delays. 

Period  No.  if. — This  period  extended  from 
June  9  to  July  i,  and  represents  three  con 
secutive  minor  rises  of  the  river.  The  period 
closed  with  the  beginning  of  a  marked  rise 
which  caused  the  water  to  become  very 
muddy. 

The  Warren,  Tewell,  and  Western  Pressure 
systems  were  regularly  in  operation  with  the 
exception  of  three  days  in  the  case  of  the 
Warren  System.  This  delay  was  caused  by 
repairs  of  a  break  in  the  agitator  machinery. 

Period  No.  18. — This  period  extended  from 
July  i  to  6.  and  represents  very  rapidly  rising 
and  falling  stages  of  the  river.  Heavy  rains 
fell  on  the  local  watershed  and  the  water  be 
came  very  muddy.  The  rise  quickly  subsided, 
and  the  period  ended  at  the  beginning  of  a 
minor  rise. 

During  this  period  the  remodeled  Western 
Gravity  System  was  put  in  operation  accord 
ing  to  a  proposition  offered  by  the  Western 
Filter  Company.  It  was  agreed  that  for  the 
balance  of  the  investigations  the  pressure  sys 
tem  was  to  be  operated  on  the  first  four  days 
of  each  week,  and  the  gravity  on  the  last  two 
days.  This  proposition  was  made  in  reply  to 
a  request  from  the  Water  Company  for  an 
official  explanation  of  the  fact  that  at  that 
time  the  Western  Gravity  System  had  been 
withdrawn  from  the  tests  for  a  period  of  more 
than  three  months.  The  communication  re 
ceived  from  the  Western  Filter  Company, 
under  date  of  June  26,  1896,  is  as  follows: 

"  The  difficulties  experienced  in  the  earlier 
part  of  the  filter  tests  occasioned  by  running 
both  our  filters  on  the  same  main  with  the 
other  filters,  which  we  hoped  to  remedy  by 
the  changes  made  in  April,  have  been  but  par 
tially  removed.  We  find  now  after  several 
unofficial  trial  runs  that,  owing  to  wide  varia 
tions  in  the  pressure  due  to  changes  in  ve 
locity  in  a  4-inch  main,  brought  about  by 
opening  and  closing  either  outlet,  it  is  liable 
to  impair  seriously  the  results  of  our  work  to 


SUMMARY  AND  DISCUSSION  OF   DATA    OF   1895-90. 


219 


run  both  filters  at  the  same  time.  We  have 
therefore  continued  the  service  of  our  pres 
sure  filter,  beliving  that  we  obtained  better 
results,  at  least  mechanically,  from  that  por 
tion  of  our  plant. 

"  \Ve  are  prepared,  however,  if  it  be  desir 
able  for  the  information  of  the  Water  Com 
pany,  to  run  our  gravity  filter  at  such  inter 
vals  and  for  such  periods  as  may  be  deemed 
advisable,  discontinuing  the  service  of  our 
pressure  filter  during  such  periods." 

Operations  of  all  systems  were  suspended 
on  July  4,  and  on  July  4  and  5  the  sand  layer 
of  the  Jewell  System  was  changed. 

Period  No.  19. — This  period  extended  from 
July  6  to  22,  and  represents  a  fairly  uniform 
stage  of  the  river  with  comparatively  muddy 
water.  Occasional  rains  on  the  local  water 
shed  caused  several  minor  rises,  but  none  of 
any  large  amount  or  extended  duration. 

The  Jewell  Svstem  was  operated  with 
higher  amounts  of  sulphate  of  alumina  than 
the  condition  of  the  water  warranted,  and 
consequently  the  effluent  of  this  system  was 
frequently  acid. 

The  Warren  System  was  in  regular  opera 
tion,  and  the  Western  Systems  were  operated 
under  the  arrangement  outlined  above. 

Period  No.  20. — This  period  extended  from 
July  22  to  the  close  of  the  investigations  on 
Aug.  i.  It  represents  the  most  marked  rise 
noted  during  the  investigations,  and  through 
out  this  period  the  river  water  contained  sus 
pended  solids  ranging  from  805  to  3347  parts 
per  million. 

Great  difficulty  was  experienced  by  all  the 
systems  in  handling  this  water,  owing  to  the 
frequent  washings  of  the  sand  layer  necessi 
tated  by  the  large  amounts  of  mud  in  the 
water  after  the  short  subsidence  and  before 
filtration.  Relatively  high  amounts  of  sul 
phate  of  alumina  were  used  with  the  view  of 
securing  satisfactory  coagulation. 

During  this  period  the  operation  of  the  sys 
tems  was  delayed  in  a  number  of  instances  in 
order  that  the  Water  Company  might  make  a 
number  of  tests  and  observations  of  an  engin 
eering  nature.  A  very  slight  excess  of  sul 
phate  of  alumina  above  the  amount  capable 
of  decomposition  by  the  river  water  was  ap 
plied  during  the  majority  of  the  period  in  the 
case  of  the  Jewell  System.  Complications  of 


a  greater  or  less  degree  arose  in  the  case  of 
the  \Varreu  System,  beginning  about  July  22, 
from  the  passage  of  sludge  from  the  settling 
basin  on  to  the  filter.  This  was  remedied  on 
July  27  by  cleaning  the  settling  basin. 

Just  how  far  this  complication  affected  the 
results  of  this  system  is  difficult  to  say.  But 
it  doubtless  caused  the  sand  layer  to  be 
washed  at  abnormally  frequent  intervals  and 
caused  a  greater  or  less  increase  in  the 
amount  of  applied  sulphate  of  alumina,  and 
something  of  a  decrease  in  bacterial  effi 
ciency. 


This  table  comprises  all  the  qantitative  and 
the  leading  qualitative  data,  arranged  and 
compiled  for  each  of  the  twenty  periods  into 
which,  as  has  already  been  explained,  the  re 
sults  of  the  investigations  are  divided.  Maxi 
mum  and  minimum  results  during  the  periods 
were  obtained  by  inspection  of  the  records 
presented  in  'fable  Xo.  5  of  Chapter  VIII. 

The  exact  significance  of  all  expressions 
not  explained  here  was  presented  in  Chapter 
VIII.  The  data  presented  in  this  table,  and 
the  methods  of  averaging  employed,  are  as 
follows: 

Periods  of  Time. — The  average  length  of 
time  per  run  included  in  the  periods  of 
"  operation,"  "  service,"  and  "  wash  "  are  ex 
pressed  in  hours  and  hundredths  of  hours. 

These  results  were  obtained  in  each  case 
by  dividing  the  total  respective  times  by  the 
number  of  runs  included  in  the  period. 

Quantities  of  Water. — The  average  quanti 
ties  of  water  per  run  are  given  in  cubic  feet. 
These  were  all  computed  by  dividing  the  re 
spective  total  quantities  for  the  period  by  the 
number  of  runs  included  in  the  period.  In  all 
computations  for  this  table  the  actual  quanti 
ties  registered  by  the  meters  were  used. 

Percentage  which  ///('  Sinn  of  the  Wash  and 
Waste  Water  was  of  the  Allied  Water.— 
These  results  were  obtained  by  dividing  the 
total  quantity  of  wash  and  waste  water  for  the 
period  by  the  total  quantity  of  applied  water. 

Actual  Rate  of  Filtration. — The  average 
actual  rate  of  filtration  in  cubic  feet  per  min- 


WATER  PURIFICATION  AT  LOUISVILLE. 


ute  was  determined  by  dividing  the  total 
quantity  of  water  registered  by  the  liltered- 
water  meter  by  the  total  period  of  service. 
These  results  are  also  given  in  million  gal 
lons  per  acre  per  twenty-four  hours  by  multi 
plication  of  the  rates  in  cubic  feet  per  minute 
by  the  proper  constants. 

Average  Net  Kate  of  Filtration. — These  re 
sults  were  obtained  by  dividing  the  difference 
between  the  quantity  of  applied  water  and  the 
quantity  of  wash  and  waste  water  by  the 
period  of  operation,  using  in  all  cases  the 
totals  for  the  period.  The  rates  in  million 
gallons  per  acre  per  twenty-four  hours  were 
obtained  from  these  rates  by  the  use  of  the 
proper  constants. 

Arc/  Quantity  of  Filtered  Jl'atcr  per  Run  in 
Million  Gallons  per  Acre. — These  results  were 
obtained  by  deducting  the  quantity  of  wash 
and  waste  water  from  the  quantity  of  the  ap 
plied  water,  and  multiplying  the  results  by  the 
proper  constant  value  of  i  cubic  foot  in  mil 
lion  gallons  per  acre.  Averages  were  ob 
tained  by  using  total  quantities  for  the  period. 
Estimated  Suspended  Solids  in  River  ll'ater. 
— Under  this  head  are  given  the  maximum  and 
the  minimum  average  amounts  of  suspended 
solids  estimated  for  the  different  runs,  and 
the  average  amount  for  the  entire  period. 
The  averages  were  obtained  by  multiplying 
the  average  solids  for  each  run  by  the  quan 
tity  of  applied  water  on  that  run,  and  dividing 
the  sum  of  these  products  by  the  total  quan 
tity  of  applied  water  for  the  period. 

Grains  of  Applied  Sulphate  of  Alumina  per 
Gallon  of  Applied  Water. — The  maximum  and 
minimum  amounts  averaged  for  any  run 
during  the  period  are  given,  and  also  the 
weighted  averages  for  the  period.  The  latter 
were  obtained  in  the  same  manner  as  the 
average  suspended  solids. 

Average  Grains  of  Applied  Sulphate  of 
Alumina  per  Gallon  of  Net  Filtered  IVatcr. — 
These  results  were  obtained  by  dividing  the 
amounts  of  sulphate  of  alumina  per  gallon 
of  applied  water  by  the  percentages  which  the 
net  filtered  water  was  of  the  applied  water, 
using  in  both  cases  averages  for  the  period. 

Degree  of  Clearness. — The  maximum,  mini 
mum  and  average  degrees  of  clearness  are 
given.  The  average  degree  given  in  each 
case  is  the  sum  of  degrees  recorded  as  aver 


ages  for  each  run  divided  by  the  number  of 
runs. 

Bacteria  per  Cubic  Centimeter  in  River 
ll'ater. — The  maximum  and  minimum  aver 
age  numbers  per  run.  and  the  average 
number  for  the  period,  of  the  bacteria  in 
the  river  water  are  given.  The  averages  were 
obtained  in  the  same  manner  as  the  average 
amounts  of  suspended  solids. 

Average,  Maximum  and  Minimum  Numbers  of 
Bacteria  per  Cubic  Centimeter  in  the  Filtered 
ll'ater. — These  results  are  actual  averages  of 
the  observations  recorded  as  maximum  and 
minimum  numbers  of  bacteria  for  the  several 
runs.  \Yhere  the  number  of  observations  was 
less  than  one  half  of  the  number  of  runs  for 
the  period  no  average  is  given. 

Average  Numbers  of  Bacteria  per  Cubic  Cen 
timeter  in  Filtered  ll'ater. — The  averages  per 
run  which  were  the  maximum  and  minimum 
during  the  period  are  given,  and  also  the 
average  number  for  the  periods.  The  aver 
ages  were  obtained  by  multiplying  the  aver 
age  for  each  run  by  the  quantity  of  filtered 
•water  on  that  run,  and  dividing  the  sum  of 
these  products  by  the  total  quantity  of  fil 
tered  water  for  the  period. 

Average  Bacterial  Efficiencies. — The  average 
efficiencies  per  run,  which  were  the  maximum 
and  minimum  for  the  period,  are  given,  and 
also  the  averages  for  the  periods.  The  latter 
were  obtained  by  dividing  the  difference  be 
tween  the  average  numbers  of  bacteria  in  the 
river  water  and  in  the  effluent  by  the  average 
numbrr  in  the  river  water,  these  averages 
having  been  determined  as  described  above. 


In  this  table  are  presented  the  total  periods 
of  time  devoted  to  operation,-service  and  pre 
paring  the  filters  for  filtration;  the  total  quan 
tities  of  water  recorded  by  the  meters;  and 
averages  of  each  of  these  periods  and  quan 
tities  per  run,  obtained  by  dividing  the  respec 
tive  total  amounts  by  the  number  of  runs. 
The  records  of  the  runs  not  included  in  aver 
ages  are  omitted  from  this  as  well  as  all  other 
tables.  There  are  presented  also  in  this  table 
the  following  averages: 

Average  Actual  Rate  of  Filtration. — These 
results  were  obtained  by  dividing  the  total 


SUMMARY  AND   DISCUSSION   OF  DATA    OJ<    1895-96. 


quantities  of  filtered  water  by  tbe  total 
periods  of  operation,  rates  in  cubic  feet  per 
minute  being  transferred  into  million  gallons 
per  acre  per  twenty-four  hours  by  the  use  of 
the  proper  constants. 

Average  Grains  of  Sulphate  of  Alumina. — • 
The  average  amounts  of  sulphate  of  alumina 
per  gallon  of  filtered  water  were  obtained  in 
each  case  by  multiplying  the  average  amount 
for  each  run  by  the  total  quantity  of  applied 
water  on  that  run,  and  dividing  the  sum  of 
these  products  by  the  total  quantity  of  ap 
plied  water.  The  average  amounts  per  gal 
lon  of  net  filtered  water  were  obtained  by  di 
viding  the  respective  amounts  per  gallon  of 
applied  water  by  the  percentages  which  the 
net  filtered  water  were  of  the  applied  water. 

Average  Bacterial  Efficiencies. — These  re 
sults  were  obtained  in  the  same  manner  as 
were  the  average  amounts  of  sulphate  of  alu 
mina  used  per  gallon  of  applied  water. 

Table  No.  6. 

In  this  table  are  given  summaries  of  the 
leading  results  obtained  from  the  entire  in 
vestigation  and  from  certain  portions  thereof. 

Summary  No.  i  includes  the  data  obtained 
during  the  entire  investigation  (excluding 
those  runs  not  included  in  averages). 

Summary  No.  2  includes  all  the  data  given 
in  Summary  No.  i,  except  those  obtained 
during  the  periods  when  the  operations  were 
under  conditions  prescribed  by  the  Water 
Company  in  regard  to  rates  of  filtration  and 
amounts  of  sulphate  of  alumina  applied 
(Periods  14,  15  and  16). 

Summary  No.  3  includes  all  the  data  used 
in  Summary  No.  2  except  those  obtained 
during  Period  No.  i,  when  the  operations  of 
the  Warren  System  were  under  protest  of  the 
Cumberland  Manufacturing  Company,  but 
were  continued  at  the  request  of  the  Water 
Company. 

Summary  No.  4  includes  the  data  from  all 
the  perio'ds  when  the  Warren,  Jewell  and 
Western  Pressure  systems  were  in  service,  ex 
cept  those  when  the  conditions  of  operation 
were  prescribed  as  noted  above. 

Summary  No.  5  includes  those  periods 
when  all  of  the  systems  were  in  operation,  ex 
cept  Periods  14,  15  and  16. 


In  this  table  the  same  expressions  which 
have  been  used  throughout  are  employed,  and 
reference  is  made  to  the  explanation  of  Table 
No.  5  of  Chapter  VIII,  where  the  exact 
significance  of  the  several  expressions  is  ex 
plained. 

The  data  presented  and  the  methods  of 
computation  employed  are  as  follows: 

The  periods  of  service  and  of  wash  are  ex 
pressed  in  percentages  of  the  period  of  opera 
tion. 

The  quantities  of  water  used  for  washing, 
the  quantities  of  filtered  water  wasted,  the 
quantities  of  unfiltered  water  wasted,  and  the 
quantities  of  effluent  are,  respectively,  ex 
pressed  in  percentages  which  they  were  of 
the  corresponding  quantities  of  water  applied 
to  the  respective  systems.  It  is  to  be  noted 
that  in  all  cases  in  this  table  the  quantity  of 
filtered  water  (effluent)  is  the  difference  be 
tween  the  applied  water  and  the  waste  water, 
and  not  the  quantity  measured  by  the 
meter. 

Average  actual  rates  are  given,  the  rates 
in  cubic  feet  per  minute  being  obtained  by 
dividing  the  total  quantity  of  effluent  by  the 
total  period  of  service.  The  rates  in  million 
gallons  per  acre  per  twenty-four  hours  were 
obtained  by  the  usual  method  of  transference 
•from  comparative  tables. 

The  average  net  rates  were  obtained  in  the 
same  manner  as  the  actual  rates,  except  that 
the  net  filtered  water  and  net  period  of  opera 
tion  were  used. 

The  average  amounts  of  sulphate  of  alu 
mina  per  gallon  of  applied  water  were  ob 
tained  in  each  case  by  multiplying  the  average 
amounts  per  run  by  the  quantity  of  applied 
water  on  that  run,  and  dividing  the  sum  of  the 
products  by  the  total  quantity  of  applied 
water.  The  amounts  per  gallon  of  net  filtered 
water  were  obtained  by  dividing  the  amounts 
per  gallon  of  applied  water  by  the  per 
centages  which  the  net  filtered  water  was  of 
the  applied  water. 

The  average  bacterial  efficiencies  were  cal 
culated  in  the  usual  manner  of  obtaining 
efficiencies,  using  for  average  numbers  of 
bacteria  results  obtained  in  the  same  manner 
as  the  average  amounts  of  sulphate  of  alu 
mina. 


222  WATER   PURIFICATION  AT  LOUISVILLE. 

TAIH.E  No.  1. 

SUMMARY    BY    DAYS    OF   THE    API'KARANCK    OF   THK   EFFLUENTS   OF   THE    RESPECTIVE    SYSTEMS, 

Expicssed  in  Decrees  of  Clearness. 


Warren 

~   . 

Jewell 

? 

.  .       2 

October 

Warren 

3   •  • 

Jewell 

November 

Wesiern  Gravity 

Warren 

•  •     4 

lewell 

December 

„ 

.  .       2 

Warren 

]  Sc/> 

Jewell 

3 

5  •  • 

Western  Gravity 

* 

Western  Pressure 

Warren 

2    .  . 

February 

Jewell  
Western  Gravity  .  . 

. 

3 

4 

7 

2 

4 

3 

2 

5 

2 

2 

3 

4 

4 

2 

2 

2 

5 

2 
I 

3 

3 
i 

2 

3 

2   .  . 
I    .  . 

T 

? 

T 

3  •  • 

•> 

? 

2    3 

Jewell    

3 

q 

o 

o 

1 

^ 

? 

2    3 

March 

, 

Western  Pressure  . 
Warren    

2 

.. 

2 

* 

2 

•; 

I 

2 

2 

I 

1 

• 

2 

2 

2 

3 

4 

4 
? 

4 

2 

2 
3 

2 

2 

2    4 

2      2 

lewell    . 

'. 

3 

0 

, 

0 

2 

2       I 

April 

. 

Warren  

7 

7 

? 

T 

i 

? 

? 

I 

? 

2      2 

Jew-11      

? 

7 

4      I 

May 

Western  Pressure  . 
Warren 

2 

2 

4 

2 

3 

2 

2 

1 

2 

3 

2 

2 

I 

I 

2 

2 

2 

5     2 

lewell 

; 

I      2 

June 

Western  Pressure  . 
Warren  

2 
I 

3 
3 

2 

2 

2 

3 

3 

2 

2 

2 

2 

4 

2 
2 

2 
2 

2 

2 
2 

2 

2 
2 

2 

: 

2 

° 

2 
2 

0 

2 

2 

2 

2 

2 

5 

2 

5 

2 

4 

2 

2 

3 

2 
7 

2      3 

2      2 
2    .  . 

July 

a 

0 

Western    Pressure  . 

3 

3 

3 

2 

2 

2 

2 

2 

2 

2 

2 

3 

3 

2 

2 

2    .  . 

SUMMARY  AND   DISCUSSION  OF  DATA    OF   1895-96. 
TABLE  No.  2. 


223 


DAILY  RESULTS  OF  THE  DETERMINATION  OF  ORGANIC  MATTER  IN  THE  OHIO  RIVER 
WATER,  EXPRESSED  IN  PARTS  PER  MILLION  OF  NITROGEN  AS  ALHUMINOID  AMMONIA, 
AND  OF  OXYGEN  CONSUMED,  RESPECTIVELY,  TOGETHER  WITH  THE  PERCENTAGES  OF 
REMOVAL  OF  ORGANIC  MATTER  BY  THE  RESPECTIVE  SYSTEMS  OF  PURIFICATION. 


Nitrogen  as 
Wa 

in  River 

Percentape 
For 

ieinova]  b) 

the  Respect 

ve  Systems 

Total 
Oxygen 

Percent 

OxyKen  Co 

alter  Exprc 

ssed  as 

Date. 

Total. 

Percentage 
which  was 

'in  River 
Water. 

Warren. 

Jewell. 

Western 

Western 

Suasion 

Grav.ty. 

66 

2$ 

,, 

,- 

l(         T 

2SS 

ifi 

,, 

2  6 

2    6 

ifi 

"      26 

71  6 

"      28 

216 

^8 

" 

* 

^6 

26 

Nov      T 

df) 

62 

48 

20 

6 

"       8 

' 

12 

22 

I   8 

I 

"     1  6 

28 

18 

18 

26 

2    8 

"     26 

.246 

^  8 

27 

•  232 

26 

11     28 

36 

28 

Dec       i 

.216 

^6 

2    6 

2    8 

18 

.216 

2.6 

6 

48 

2    8 

"       7 

8 

.234 

46 

63 

67 

.184 

56 

"     ii 

65 

"     T3 

.158 

24 

50 

48 

224 


WATER  PURIFICATION  AT  LOUISVILLE. 
TABLE  No.  2. — Continued. 


Wa 

in  River 

I'crcentape 
of  Organic  r 

Mailer  Expr 
m  of  Album 

essed  as  Nitr 

o"en  in  the" 

Oxygen 

Sysums 

if  Organic  N 
Oxygen  Co 

utter  Exprt 

ssecl  as 

Date. 

PercentaRe 

in  River 

Suspension 

Gravity. 

Gravity. 

1895 

Dec.  14 

36 

3-  5 

28 

"     16 

188 

"     17 

48 

"     18 

.228 

60 

4s 

"     26 

"     28 

Av.  27-30 

.388 

6l 

75 

79 

79 

79 

6.0 

70 

77 

77 

73 

1896 

2 

"       3 

1.187 
1.187 

83 
S3 

89 

89 
89 

93 
93 

92 
92 

12.3 
ii.  8 

......... 

88 
87 

84 

84 

89 
87 
89 

86 
90 
86 

Av.  4&  6 

.6=3 

76 

82 

88 

88 

7  8 

83 

82 

Ian.    7 

6  5 

83 

Av.  8,9,10 
Jan.    it 

\    -423 
( 
.261 

48 
45 

74 

72 

68 
63 

73 
65 

72 
6  1 

5-4 
5-8 
5-3 

65 

S3 
Si 

67 
72 
72 

65 
69 

75 

67 
72 
74 

Av.  14,  15 
Jan.    16 

]     -209 

12 

86 

62 

62 

54 

4-1 
4-1 

6  1 

73 

76 
63 

76 
61 

66 

58 

"      T7 

"      18 

6  1 

"       22 

•  135 

7 

56 

50 

47 

47 

3-1 

61 

55 

45 

52 

"       24 

"       25 

"       20 

Av.  27,  28 

j     .369 

70 
Si 

Si 
81 

70 

74 

76 

5-5 
6.6 

78 
77 
82 

69 
64 

78 
68 

75 
74 

"     3° 

"     31 

Feb.     i 

.365 

8« 

Sq 

6.6 

85 

82 

So 

"          2 

"       3 

67 

8-3 

go 

83 

83 

83 

85 

82 

82 

84 

81 

81 

5 
6 
7 
"        8 

•439 
.417 

•593 

Si 

81 
87 
Si 

86 
88 
93 

84 
86 
93 

85 
83 
90 

84 
82 
90 

8.4 

8.2 
ii.  4 

82 
88 
91 

86 
84 
90 

85 

83 
84 
87 

83 
So 
87 

"       9 

"        10 

•577 

88 

94 

92 

94 

93 

12.8 
fi    Q 

91 

88 
84 

91 

88 

91 

87 

76 

88 

88 

!     T3 

.215 

60 

78 

33 
80 

So 

8  i 

76 

78 

4-6 
7  6 

78 
85 

70 

74 

78 

"     15 

•353 

-8 

91 

84 

87 

.        85 

8.7 

87 

84 

87 

85 

SUMMARY  AND   DISCUSSJON   OF  DATA    Ol<~   1895-96. 


225 


TABLE  No.  2. — Continued. 


Nitrogen  a 
raon 

Albuminoi 
ter. 

Percentage 
Ki 

Removal  bj 
nn  of  Albui 

the  Respei 
linoid  A  mm 

live  System 

Total 

Ox  v  gen 

I',  n  nil 

...    Krm    v 
OxyKcn  C 

by  the  Res 

^ective 
ssed  as 

Date. 

Total. 

rcrccntiiK 
iSuspTnsio 

Warren. 

Jewell. 

Western 
Gravity. 

Western 
Pressure. 

in  River 

Water. 

Warren. 

Jewell. 

Western 
Gravity. 

Western 

1896 
Feb.  16 

"     I? 

"     18 

.292 
.366 

75 

86 
95 

82 

»4 

84 

7-5 

88 

S3 
85 

88 

»7 

"     19 
"     20 

.484 

.232 

88 

95 
84 

94 

86 

92 

84 

II.  2 

6   -\ 

92 

86 

91 

8q 

92 

79 

"       21 
22 

.256 
.288 

81 
76 

92 

87 

86 

82 

85 

87 

7.2 

6  o 

90 

87 

90 

So 

S7 

86 

"       23 

"       24 

"       25 

.162 
•  152 

69 
64 

79 
71 

74 
67 

78 

78 

4-3 

3  s 

84 
82 

74 
63 

79 

72 

"       26 
"       27 

.146 
.200 

71 

70 

82 

73 

78 

78 

75 

3-3 

79 
82 

64 
82 

76 

76 

"       28 

"       29 

Mar.     I 

.102 
.088 

35 
43 

57 
73 

51 

55 

i* 

j  68 

3-0 

2.8 

70 
64 

57 
54 

!„ 

I'" 

2 

3 

.084 
.118 

50 
53 

64 
68 

5" 
68 

52 

52 

2.6 

73 

Si 

42 
63 

65 

62 

4 

5 

.088 
.  IOO 

57 
48 

61 
74 

50 
60 

64 

66 

2-5 

72 
62 

44 

60 

64 

"       6 
7 
8 

.184 

.  IO2 

36 
46 

76 

78 

45 
7i 

i« 

f« 

1.8 

2.5 

76 

56 
68 

i'" 

i" 

9 
10 

.076 
.OgO 

53 
51 

68 
62 

68 
69 

63 

66 

2.3 

61 

70 
68 

65 

7" 

"     n 
"       12 

.096 

.116 

46 

38 

73 
74 

65 
69 

65 

j  48 

i 

i.  9 

79 

63 
6^ 

63 

* 

"     '3 
'      M 
"     15 

.094 
.108 

49 
54 

68 
65 

64 
67 

{64 

I" 

2.  I 
2-3 

67 
65 

52 
65 

{» 

j, 

"      16 
"     '7 

.  no 
•  130 

42 
58 

75 
77 

60 

68 

53 

67 
( 

2  .  5 

72 

60 

60 

64 
( 

•     i- 

'     19 

"     20 

"      21 

.132 

.238 

.700 
1  .046 

50 
73 
90 

74 
79 
95 

74 
77 
93 

i" 

95 

\« 
I* 

3-0 
5-0 
14.2 

17    R 

73 
82 
94 

73 
So 
89 

{» 

91 

i" 
i* 

"      22 

"      23 

.580 

86 

88 

"      24 

.476 

86 

92 

"      25 

.414 

86 

8  i 

"      26 

.462 

85 

89 

8    Q 

So 

"      27 

•344 

78 

87 

83 

86 

So 

Sj 

88 

"      28 

•454 

84 

88 

80 

8  3 

80 

80 

"      29 

•  374 

79 

S5 

82 

86 

88 

88 

88 

"     3° 

.852 

87 

95 

"     31 

.932 

April     I 

1  .032 

96 

06 

TC:   8 

2 

.960 

93 

97 

96 

15  6 

06 

3 

1.080 

93 

96 

96 

18  4 

06 

06 

4 

.620 

84 

94 

5 

6 

.500 

83 

90 

8  6 

7 

.380 

81 

90 

"       8 

.370 

75 

85 

85 

6  7 

88 

88 

9 

.380 

79 

88 

88 

"     10 

.312 

74 

85 

82 

6   -* 

86 

84 

"     n 

.286 

72 

78 

82 

6  5 

83 

86 

"       12 

"     T3 

.270 

68 

80 

'     14 

.166 

53 

66 

60 

"     15 

.208 

62 

69 

78 

"     16 

.164 

50 

66 

T    6 

6n 

"     17 

•  172 

51 

63 

'     18 

.206 

52 

64 

"     T9 

WATER  PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  2. — Continued. 


Nitrogen  as 

Wa 

in  River 
ter. 

Percentage 
of  Organ! 
the  F 

Removal  bv 
Matter  Kx| 
jrm  of  Albu 

the  Respect 
ressed  as  N 

«  Systems 

Total 
Oxygen 

Percent  a 
Systems 

ge  Removal 

of  Organic 
isOxygenC 

by  the  Resp 
Matter  Expr 

ective 

essed 

Date. 

Total. 

Percentage 

which  was 

Suspension 

Warren. 

Jewell. 

Western 
Gravity. 

Western 
Pressure. 

in'  River 

Water. 

Warren. 

Jewell. 

Western 
Gravuy. 

Western 
Pressure 

1896 

198 

81 

'• 

188 

66 

66 

go 

56 

61 

81 

118 

65 

6s 

i  16 

2  8 

*8 

"      26 

68 

68 

"      28 

67 

6a 

64 

58 

67 

67 

65 

60 

1  68 

48 

67 

68 

60 

188 

60 

67 

i  6 

65 

i  6 

60 

6 

.188 

68 

69 

68 

68 

.164 

61 

63 

"       8 

62 

fie 

60 

63 

58 

68 

.286 

66 

84 

Si 

7,S 

go 

68 

2-»6 

65 

72 

fil 

66 

65 

76 

7S 

62 

182 

60 

76 

75 

i  6 

67 

"     if) 

60 

60 

68 

75 

"      18 

cS 

52 

"      '9 

.158 

59 

56 

,s 

61 

35 

228 

62 

73 

68 

68 

63 

58 

6S 

fie 

i  $ 

66 

55 

"       22 

.228 

61 

70 

66 

"      23 

6c* 

68* 

"      25 

.166 

58 

cfi 

"      26 

.158 

58 

58 

( 

( 

"       27 

.186 

58 

69 

66 

\n 

67 

67 

l?3 

"      28 

.566 

79 

86 

85 

8  4 

83 

83 

( 

"      29 

.602 

78 

87 

87 

ST 

g7 

81 

"     3° 

.502 

76 

86 

88 

7   8 

8=1 

37 

"     31 



June    i 

.446 

76 

84 

86f 

83 



86f 

.576 

89 

87 

8  o 

88 

86 

84 

"       3 

67 

86 

S5 

^i 

c  R 

8d 

84 



84 

"       4 

.324 

69 

80 

Si 

Si 

83 

83 

83 

"       5 

.274 

54 

74 

( 

76 

81 

1  , 

6 

48 

74 

67 

1     ; 

"       7 

8 

"       9 

.404 

So 

83 

85 

( 

6  S 

Si 

84 

( 

"       10 

.340 

72 

Si 

82 

J82 

6  i 

80 

84 

>7 

"      it 

.282 

68 

r 

76 

( 

"       12 

.250 

65 

70 

68 

76 

"      '3 

.232 

<J3 

72 

76  1 

67 

7<4 

"     14 

"     15 

•  364 

74 

79 

So 

=;  6 

"      16 

.248 

64 

69 

67 

"      '7 

.260 

65 

69 

i  6 

65 

73^ 

"     18 

.288 

67 

72 

76 

64 

78 

"      T9 

.392 

72 

83 

81 

( 

78 

1 

"      20 

.268 

66 

74 

75 

J8, 

4-3 

f)0 

65 

j  73 

'  Average  for  22,  23,  and  25. 


f  Average  May  30  and  June  I. 
§  Average  16,  17,  and  18. 


|  Average  12,  13,  and  15. 


SUMMARY  AND    DISCUSSION  OF  DATA    OF   1895-96. 
TAULE  No.  2. — Concluded. 


22-J 


Date. 

Nitrogen  as  Albuminoid 
Water. 

Percentage  Removal  by  the  Respective  Systems 
of  Organic  Matter  Kxpressed  as  Nitrogen  in 
the  Form  of  Albuminoid  Ammonia. 

Total 

Consumed 
in  River 
Water. 

Percentage  Kemova  by  the  Respective 

Systems  of  Organic  Matt,  r  Kxpressed 
as  Oxygen  Consumed. 

Total. 

Percentage 

Suspension 

Gr.mty. 

I  ressure.  ^ 

1896 
June  21 
"      22 

"     23 
"     24 
"     25 

'•    26 
"    27 
"    28 

"      29 

"   30 

July     I 

2 
"       3 

4 
5 

"       6 
7 
"       8 
9 

'       10 

"     ii 

"       12 
"       13 
'      M 

"      15 

"     16 
"     17 
"     18 
"     19 

'      20 
"       21 
"       22 

"       23 
"       24 
"       25 
"       26 
"       27 
"      28 
"      29 

"     3° 
"     3i 

.222 
.224 
.460 
.326 
•304 

•374 

53 
55 
77 
65 
62 
67 

67 
65 
So 

67 
62 
79 

4.0 
3-7 
5-1 
6  o 

63 
70 

73 

67 

f'5 
71 

(o 

i» 

i: 

78 
So 

1  80 

J79 

5-1 

5-5 

7i 

78 

•442 
.356 
.628 
.964 
.640 

71 

72 
82 
89 
83 

84 
82 
9' 
93 
90 

1 

7-4 
5.6 
10.7 
15.0 

12.  I 

86 
So 
9' 
91 
90 

79 
88 
92 
89 

73 
88 

9i 
89 

86* 

83*. 

92 
89 

90 
90 

.258 
.398 
•432 
•378 
.346 
.224 

57 
74 
75 
72 
•63 
52 

69 
83 
83 
80 
79 
73 

74 
83 

i" 

81 
73 

1" 

{,0 

4.8 
7-o 
6.8 

6.6 

5.8 
4-,4 

73 

84 
82 
83 
79 

77 

81 

84 

!» 

88 
82 

i'" 

i" 

"P" 

J76 

.382 
.310 
.420 
-378 
•394 
•504 

72 

66 
70 
76 
79 
81 

80 
77 
81 

84 

1" 

84 
82 
84 
84 

{,, 

i" 
i* 

7.0 
6.6 

8.3 
7-0 
7.0 

8.7 

S3 
82 
84 
86 

i'< 

87 
86 
89 
87 

(- 

t'.; 

j  86 

|  86 

i« 

-318 
•494 
.824 
1  .360 
2.400 
i  .  320 

70 
78 
89 
90 
95 
91 

81 
85 
90 

91 
96 

93 

84 
87 
92 
94 
97 
96 

jji 
i« 

6.'s 

7-7 
14.9 
24.8 
35.8 
22.6 

82 
84 
90 

93 
96 
92 

86 
87 
92 
95 
97 
95 

j',5 

|« 

!»"' 

{95 

i.  200 

I.  120 
.880 
I.2OO 
.470 

89 
89 
85 
90 
75 

93 
94 
92 

!" 

95 
94 
92 

|« 

21.7 
17.8 

T9-7 
23.4 

13-6 

93 
92 
9i 

),3 

95 
93 
91 

1"' 

84 

9o 

Average  June  30,  July  I. 


228 


WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE  No.  3. 

AVERAGE  DAILY  NUMBER  OF  BACTERIA  PER  CUBIC  CENTIMETER,  IN  THE  OHIO  RIVER 
WATER  AND  IN  THE  SEVERAL  EFFLUENTS,  TOGETHER  WITH  THE  AVERAGE  BACTERIAL 
EFFICIENCY  OF  THE  RESPECTIVE  SYSTEMS  OF  PURIFICATION. 


SUMMARY  AND   DISCUSSION  OF  DATA    OF   1895-96. 
TABLE  No.  3. —  Continued. 


229 


1895 

Dec.  27 


Jan. 


Mar. 


Bacteria 

pel  (  ubi  (  ,  n 

i  meter. 

Eff 

uents  of  the  R 

jspective  Syste 

ms. 

River  Water. 

\Vcst.  in 

Western 

Western 

W.-  •  i 

12  OOO 

35  7oo 

779 
i  169 

410 

813 

501 
947 

358 
897 

93-5 
76.7 

96.6 
97-7 

95-8 
97-3 

97.0 
97-5 

12  OOO 

13  ooo 

328 
375 

3" 

233 

529 
253 

409 
263 

97-3 
97.1 

97-4 
98.2 

95-6 
98.1 

96.6 
97-9 

10  700 
14300 
8600 

797 
1  66 

151 

261 
343 
390 

245 
325 
Si 

258 
169 

TOO 

92.6 
98.8 
98.2 

97.6 
97.6 
95-5 

97-7 
97-7 
99.  i 

97.6 
98.8 

98.8 

368 

9"  6 

98  7 

97  S 

98  i 

4  loo 

59 

98  6 

96  .  3 

I  goo 
I  800 

2  500 

28 
94 
36 

229 
202 
152 

100 

108 
94 

78 
151 
153 

98-5 
94.8 
98.6 

87.9 
88.8 
93-9 

94-7 
94-u 
96.2 

95-9 
91.6 

93-9 

38 

98  o 

89  8 

800 
3000 
3  200 
6  500 

73<» 

25 
50 
73 
98 
60 

156 
156 
181 
262 
189 

6  1 
128 
130 

159 

228 

88 
M7 
122 
219 
244 

96.9 
98.3 
97-7 
98.5 
99.2 

80.5 
94.8 
94-3 
96  .  o 
97-4 

92.4 
95-7 
95-9 
97.6 
96.9 

89.0 
95-1 
96.2 
96.6 
96.6 

6  400 
3000 
2  6oO 

119 
5i 
34 

229 
170 
104 

219 
174 
192 

68 

218 

194 
120 
T76 

98.  i 
98.3 
98.7 

96.4 

94-3 
96  .  o 

96.6 
94-2 
92.6 
qS.6 

96.6 
93-5 
95-4 
96  3 

3  600 

06 

06  i 

7  200 

60 

"7 

102 

136 

99-2 

98.4 

98.6 

98.1 

10600 

14700 

1  8  200 

J56 
470 
525 

945 
I  533 

651 

i  5«6 

747 
876 

98.5 
96.8 

91.1 
89.6 

93-9 
89.2 

93.0 
94-0 

23  400 

72 

820 

14300 

21  3OO 

57 
56 

860 

549 

475 
188 

99.6 

94.0 

96.2 

96.7 

62  200 

197 

55  ooo 

8ie 

98  5 

71  ooo 
30  800 
55000 
29  800 

583 

220 
362 
365 

643 
I  563 
639 
i  395 

548 
805 
i  200 
669 

686 
I4f>i 

967 
7M 

99.2 
99-3 
99-3 

98.8 

99.1 
94-9 

98.8 
95-3 

99-2 
97-4 
97.8 
97-8 

99-o 
95-3 
98.2 
97.6 

14400 
19  800 

279 

740 

37i 

527 
180 

98.1 

94-9 

97-4 

96-3 
98  i 

28  ooo 

98  5 

98.7 

14  800 
ii  goo 
10  800 

430 
589 
139 

549 

848 
763 

453 
340 
950 

409 
216 
850 

97-1 
95-1 
98.7 

96.9 

92-9 
92.9 

96.9 
97-1 
91.2 

97-2 
98.2 
92.1 

21  800 
14400 

20  700 
17400 

10  700 
20  ooo 

107 
80 
'45 

210 
76 

I  079 
I  581 
919 
341 
318 

789 
647 
467 
291 
189 

638 
710 
547 
532 
169 

99-5 
99.4 
99-3 
98.8 
99-3 

95-1 
89.1 
95-6 
gS.o 
97.0 

96.4 
95-5 
97-7 
98-3 
98.2 

97-1 
95-1 
97-4 
96.9 
98-4 

15  ooo 
16  200 
25  200 
4  loo 
4500 
14  800 

73 
71 
202 
65 
156 
178 

821 
M5I 
1941 
768 
I  575 
I  601 

236 

I  012 
654 
476 

353 
f>5i 

497 
951 
574 
676 
533 
903 

99-5 
99.6 
99.2 
98.4 
96-5 
98.8 

94-5 
91.0 
92-3 
81.3 
65.0 
89.2 

98.4 
93-8 
97-4 
88.4 
92.2 
95.6 

96.7 
94.1 
97-7 
83.5 
88.2 
93-9 

44600 
33400 
29  800 
18000 

12  2OO 

10  500 

367 

302 
548 
3/1 
207 
1  80 

2  148 
1324 
851 
718 
299 
I46 

i  944 
i  062 
693 

797 
343 
332 

2  251 

798 

6ia 

615 
326 
470 

99-2 
99.1 
98.2 
97-9 
98.3 
98.3 

95-2 
96.0 
97-2 
96.0 
97.6 
98.6 

95-  (' 
96.8 
97-7 
95-6 
97-2 
96.8 

95  o 
97.6 

97-9 
96.6 

97-3 
95-5 

23° 


WATER    PURIFICATION   AT  LOUISVILLE. 
TABLE  No.   3. — Continued. 


Date. 

Bacteria  per  Culiic  Centimeter. 

Bacteria!  Efficiency  of  the  Respective  Systems. 

River  Water. 

Effluents  nf  the  Respective  Systems. 

Warren. 

Jewel.. 

Western             Western 
Gravity.             Pressure. 

Warren.             Jewell. 

Western 
Gravity. 

Western 
Pressure. 

IS96 

Mar.  8 

9 
'     10 
"     IT 

L"    I2 

"    13 
'    M 

'    15 

"     1  6 
"     17 
'      IS 
"      19 
"      20 

"      23 

1      ~4 
-5 
"      26 

"  2" 
29 

'     3" 
"     3i 
April    i 

3 

4 
5 
6 

8 
9 

'        IU 

"      1  1 

"      13 
'      M 
"      '5 
"      if> 
"      T7 
"      1  8 
"      19 

'       20 
"       21 

"       23 
'       24 
'       25 
'       26 

"       27 

"      28 

"    29 
"    30 

May    I 

"        3 
4 
5 
6 

7 
8 
9 

'        [0 

"      II 
'       12 
"       13 
'       14 
'       15 
"       If) 
"       17 
'      18 

'      '9 

14  ooo 
II  500 
7700 
I  300 

I  OOO 
2   IOO 

190 
301 

156 
293 
161 

-33 
137 
121 
251 

547 
203 

409 
2OO 
I  SO 
If)2 
233 
140 

239 

221 
If)9 

372 
162 
!59 

98.6                99-O 
97.4                98.8 
9/.I                 98.4 
98  .  6               97.8 
97-3              95-0 
98.7              98.3 

97.1 
98.3 
97-7 
98.6 
97-9 
98.8 

98.3 
98.1 
97.8 
96.7 
98.5 
98.7 

6  600 
6  300 

9  700 
4400 
46  700 
57  200 

76 
31 
49 

122 

137 
2f)0 

172 
86 
35 
7"' 
850 
928 

252 
3<)2 
520 

606 

733 

349 
37" 
441 
Soo 
55" 
I  087 

99-5 
99.8 
99.8 
99.6 
99-7 
99-5 

99.0 
99-5 
99-8 

98  '.2 
98.4 

98.5 
98.  1 
97-4 
98.2 
98.4 

97-9 
97-7 
97.8 
97-7 
98.  8 
98.1 

30  500 
37300 
46  ooo 
47  900 
31  900 
34  i"" 
49200 
25  7<->o 
26  700 
39  600 
27  500 
31  oco 
27  ooo 

If,4 

''4 
103 
136 
141 
in 
123 
125 
3^9 
263 
155 
82 
116 

844 
321 
182 
53i 
466 
,64 

379 
679 

S45 
638 
223 
20  1 

7i 

935 
368 
404 
256 
294 
537 

2  221 
I  712 
I  62S 
I  023 

755 
940 

185 

99-5 
99  -S 
99.8 

99-7 
99.6 

99-7 
99.8 
99-5 
98.6 
99-3 
99-4 
99-7 
99  •(' 

97-2 
99   1 
99.6 
98.9 
98.5 
99-5 
99-2 
97-4 
96.8 
98.4 
99.2 
99  •  3 
99  •  7 

96.9 
99.0 
99.1 
99-5 
99.  1 
98.4 
95-5 
93-3 
93-9 
97-4 
97-3 
97-0 
99-3 

1  8  700 
18  500 
13  Soo 

21  OOO 

7300 

13  ooo 

34 
40 
105 
nS 
42 
25 

3i 
64 
129 
164 
40 
4i 

91 

76 

99.8 
99.  S 

99.8 
99-7 

99-5 
99.6 

99  •  4 
99.8 

96-5 
99-7 

9  600 
7  5oo 
3  7°° 
i  700 
3  ooo 
5  9°° 

28 

QO  6 

, 

33 

98  3 

| 

4  Soo 
4  ooo 
5  5"0 
4400 
7  7°° 
8  300 

34 
82 
1  66 
no 
348 
309 

126 
16 
23 
46 

48 

99-3 
98.0 
97.0 
97-5 
95-5 
96.3 

99-9 
99-7 
99-7 
99-5 
99.4 

99  •  4 

6  500 
6  100 
7  loo 
4  100 
5400 
7  loo 

401 
605 
I3S 
94 
104 
157 

62 
1  60 
64 
42 
6  1 
78 

93-8 
90.  i 
98.1 
97-7 
98.1 
97-8 

99.0 
97-4 
99.1 
99.0 
98.9 
98.9 

i 

7  ooo 
6  ooo 
5  ooo 
5  200 
4000 
5  900 

55 
57 
S7 
76 
50 
49 

52 
45 
48 
34 
17 
39 

99.2 
99.1 
98-3 
9S.5- 
98.8 
99-2 

99-3 
99-2 
99.0 
99-3 
99.6 
99-3 

145 
20  1 

227 

97-2 
95.0 
96.2 

7300 
5  9"0 
3  600 
6  500 
6  400 
7  300 

44 
61 

12 

37 
25 
10 

32 
16 
10 
37 
27 
17 

176 
153 
167 
in 
i'7 

99-4 
99.0 
99-7 
99.4 
99.6 
99.9 

99.6 
99-7 
99-7 
99.4 
99.6 
99-8 

96.8 
97.0 
95-8 
97-4 
98-3 
98.4 

6  600 
4300 

1  20 

81 

75 
93 

701 
324 

98.2 
98.  i 

98.9 
97.8 

89.4 
92-5 

SUMMARY  AND   DISCUSSION  OF   DATA    OF   1895-96. 
TABLE  No.  3. — Concluded. 


23' 


Dale. 

Mucteria  per  Cubic  Centimeter. 

Bacterial  Efficiency  of  the  Respective  Systems. 

River  Water. 

KfHuents  of  Ihe  Respective  Systems 

Western 

Western 

Jewe.1       '      S™ 

Western 

lS(/> 
May  20 

"      21 
"      22 
"      23 

"      24 
"      25 
"      26 

"     27 

"      2S 

"    29 
"    30 
"    31 

June     I 

2 

"       3 
4 
"       5 
"       6 
"       7 
••       S 

"       9 

"       10 

"     it 

"       12 
"       13 
"       >4 
"       15 

••      16 
"     "7 
"     18 
"     19 

"      20 
"      21 

"       22 

"     23 
"      24 
"      25 
"      26 
"      27 
"      28 
"      2g 
"      30 
July     I 

2 

3 

4 
5 
6 
"       7 

"       8 
"       9 

'        10 

"      II 

"       12 
"       13 
'       M 
'       15 
'      16 
"      17 
"      IS 
'      '9 
"      20 

"       21 
"       22 
"       23 
"      24 
"      25 
"      26 
"      27 
"      28 
"      29 
"      30 
"      31 

4800 
6  100 
5  100 
6  too 

66 
70 
5" 

73 
73 
70 

2s 

184 
124 
60 
59 

98.6 
98.9 
99-0 

98.4        J- 
98.8 
08  6 

96.2 
98.0 
98.8 
99.0 

I  900 

I  800 
4  loo 
23400 
26  too 
19  700 

4' 
39 
130 

IO2 

179 
92 

59 
50 
S4 
194 
245 
322 

94 
82 
119 
261 

150 

57 

97.8 
97.8 
96.8 
99-6 
99-3 
99-5 

Of)    0 

95.1 
95-4 
97-1 
98.9 
99-4 
99-7 

gg   O              

Q9.  2 

99.  1 

f.Q      | 

18  800 
15  5oo 
13  800 
8  500 
6  400 
4900 

6  1 

101 

45 
36 

28 
25 

165 
93 
60 
93 
36 
44 

99-7 
99-3 
99-7 
99.6 
99.6 
99-5 

99-  1 
99-4 
99.6 
98.9 
99-4 
99.1 

208 

53 
45 
28 
IS 

98.7 
99.6 

99-5 
99.6 
99.6 

ii  300 
10  700 
6600 
6  too 

13400 

165 

49 
42 
40 

188 

104 
II 

TO 
II 

4" 

121 

54 
1  1 
14 
93 

98.5 
99-5 
99-4 
99-3 
98.6 

99-2 
99-9 
99.8 

98.9 
99-5 
99.8 
99.8 
99-3 

99-7 

13500 

8400 

II  OOO 

10600 
18000 
10  500 

132 
3<> 
74 
81 
73 
86 

16 

7 

27 
33 
30 
161 
30 
73 

99.0 
99-  6 
99-3 
99.2 
99.6 
99.2 

99-9 
99-9 

99-8 
99.  f> 
99-7 
08  u 

20 

53 
Si 

99.8 
99-7 
99-2 

99.8 
99-3 

7  7<» 
8000 
S  300 
7  500 
6  (xx> 
10  800 

So 
141 

234 

52 

86 

118 

453 
550 

37 

56                  (,8.9 

98.9         99-3 
(j8  5            

2lS 
'        3"5 
51 

97.2 
99-3 

94-5 

97-4 
95-9 
99.2 
'  97-7 

13300 
10900 


37 

8 
5 

43 
33 

99-7 
99-7 

99-7 

99-9       !  

24  200 
12  OOO 

95 

80 

72 
16 

83 
42 

99.6 
99-3 

99-7 
99-9 

99-7 
99.6 

7400 

5  BOO 
6  700 
9  200 

IOOOO 

9  6<x> 

64 

S2 
69 
53 
71 
40 

353 
480 
99 

10 

40 
24 

48 
3" 

21 
60 

99-  1 
93.5 
99.0 
99-4 
99-3 
99-6 

95-1 
91-3 
98.5 
99-9 
99.6 

99-7 

99-3 
99-4 
99-7 
99-4 

no 
208 

98.9 
97.8 

7  7<x> 

IO  IOO 

8  300 
5  5<*> 
5  /oo 
9  9<x> 

64 

33 
30 

3" 
ii 

23 

44 
6 
8 
II 

5 
34 

78 
25 

1  1 

18 

99-2 
99-7 
99-6 
99-4 
99-8 
99-8 

99-4 
99-9 
99-9 
99.  S 

99-9 
99-7 

99.0 
98.2 
99-9 
99-7 

33 
48 

99-4 
99-5 

7  ooo 
17  100 
33800 
27  100 
31  O'xj 
17  300 

24 
"3 

752 
597 
I  327 
433 

9 
47 
251 
103 

71 
54 

22 
204 
623 

99-7 
99-3 
97-8 
97-8 
95-7 
97-5 

99-9 
99-7 
'99-3 
99.6 
99.8 
99-7 

99-7 
98.8 
98.2 

234 
284 

99-2 
98.4 

I78<X) 
24500 
9500 
1  2  OOO 
6800 

306 
60 

52 

12 

33 

19 

6 
15 

151 
156     , 
137 

98.3 
99-8 
99-5 
99-9 

99-9 
T)9.r, 

99.  S 
99-9 

99-2 
99-4 
98.6 

f 

232 


WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE 
SUMMARIES  OF 

Warren 


NumlxT  <->f  period  

1 

2 

3 

4 

5 

6 

7 

8 

(  T);lte 

)ct.2I,'95 

Nov.  25 

Dec.  26 

an.  1  3.  '96 

Jan.  27 

Feb.  6 

Feb.  13 

Feb.  27 

X  "''"  |  Hour 

O.OOA.M. 

9-45  A.M. 

I.I7  A.M. 

2.75  P.M. 

I.O7  A.M. 

2.  36  P.  M. 

1.  1  I  P.  M. 

•  5°  P.M. 

T,    ,                                                       Date 
Kndcd                         «  ,  , 

fov.25,'95 

Dec.  26 

11.13,  '96 

Jan.  27 

Feb.  6 

Feb.  13 

Feb.  27 

Mar.  20 

(  Hour 

9.45  A.M. 

I.I7A.M. 

2.15  P.M. 

[1.  07  A.M. 

2.36  P.M. 

2.  II  P.M. 

..  5O  P.M. 

l.OO  A.M. 

Runs   inch  ded  in  period                

I—I4 

I  S—  ^1 

32—5O 

51-65 

66-78 

79-84 

85-100 

IOI-I35 

i  Maximum 

12.  OS 

23.32 

12.33 

7.18 

8.70 

6.78 

8.35 

6.07 

Minimum 

4.83 

6.5S 

3.60 

3.62 

3.18 

3-97 

3-45 

2-43 

Average 

8.87 

11.22 

5.98 

5-10 

5-82 

5.27 

5.72 

4.32 

(  Maximum 

11.83 

22.87 

12.08 

6.33 

8.03 

5.80 

8.07 

5.78 

Period  of  service.     (I  lours.  )..}  Minimum 

4.58 

6.03 

3.28 

3-07 

2.62 

3-35 

2.87 

2.15 

(  Average 

8.58 

IO.72 

5.50 

4.50 

5-15 

4-59 

5-25 

3-97 

j  Maximum 

0.42 

0.78 

1.03 

0.73 

0.92 

0.98 

o.6S 

o.55 

Period  of  wash.      (Hours.)..  .  -]  Minimum 

0.17 

0.15 

0.25 

o.53 

0.57 

0.58 

0.28 

0.22 

(  Average 

0.28 

O.5O 

0.48 

0.60 

0.67 

o.6S 

0.47 

0-35 

Ouantitv  of  applied  water.         \  ^i'"1'-""""1 
(Cul)ic  feet.) 

16  970 

7  599 

32  IO2 

8791 

16480 

3  597 

7704 

3285 

Soil 
2771 

6082 
3683 

8719 
3842 

8401 

(  Average 

n  816 

14944 

6  685 

4  749 

5  3<>7 

4  788 

(JIIQ 

5  379 

(L)uantitv  of  filtered  water.          \  M'lx.lmum 
(Cubic  feet  i 

1  6  640 
7359 

31  048 

8  126 

15  853 
3  139 

6472 

2  798 

7487 
2092 

3258 

8491 
3614 

8  182 
2885 

(  Average 

ii  457 

14   OO7 

6215 

4  if>5 

4  745 

4  286 

5  735 

5171 

Quantity  of  wash  water.             \  ^i-',^','",1™ 

741 
283 

54° 
297 

723 
271 

479 
244 

586 
432 

572 
437 

5f>i 
295 

i  286 
421 

(Cubicfcet-)  (Average 

360 

376 

374 

298 

497 

485 

446 

509 

Quantity   of   filtered    waste       \  \^™™™ 

o 

0 

469 
o 

453 
o 

440 

198 

466 
219 

407 
234 

493 

0 

202 
O 

water.      (Cubic  feet.)  |  Averagl. 

o 

221 

M4 

258 

253 

278 

M5 

IO 

Quantity  of  unfdtered  waste       \  J^*-™^ 
water       (Cubic  feet  )          .  .  ) 

400 
250 

450 

I  So 

300 
i  So 

400 
i  So 

250 
i  So 

250 
180 

300 

1  80 

300 
If,7 

181 

312 

2O6 

198 

218 

197 

2  2O 

219 

Percentage  which  wash  and      (  Maximum 

IO 

10 

26 

31 

24 

26 

32 

waste  water  was  of  applied   i  Minimum 

4 

2 

4 

13 

12 

17 

9 

S 

water             .  .             (  Average 

fa 

ii 

16 

IS 

21 

13 

13 

26.8 

25.5 

23.6 

17.  i 

If).  8 

16.3 

23.2 

25.0 

Actual           Cubic  feet  per  min.  \  Minimum 

19.8 

19.2 

14.6 

'4-7 

13.3 

I5-I 

1  6.  8 

17.6 

rate  of                                             (  Average 

22.3 

21.  8 

18.9 

15.4 

15.4 

IS-  f' 

lS.2 

21-7 

filtra-                                               (  Maximun 

tion             Mil-8als'Peracre)  Minimum 

]>er  24  hours.  .  .  |  Aye       c 

147 
109 

122 

155 
I  if) 
132 

144 
89 
114 

104 

89 
93 

IO2 
Si 

93 

99 
92 
95 

MI 
102 

no 

152 
107 
131 

Ave.  net  rate  j  Cubic  feet  per  minute  

2O.9 

20.0 

16.6 

13.0 

12.5 

12.  0 

15.5 

IS.  I 

of  filtration,  j  Mil.  gals,  per  acre  per  24  hr 

"5 

121 

101 

79 

76 

73 

94 

no 

Net  quantity  of  filtered  water  (  Maximun 

68 

131 

66 

27 

29 

21 

3i 

32 

per  run,    in  mil.    gals,    per  J  Minimum 

30 

33 

12 

n 

8 

12 

12 

IO 

acre         (  Average 

46 

59 

2f) 

17 

18 

16 

22 

20 

Average  estimated  suspended  (  Maximun 

22 

5" 

870 

IOO 

461 

967 

486 

210 

solids  in  river  water.  (Parts  •!  Minimum 

4 

15 

IOO 

20 

200 

550 

I36 

22 

per  million  )                         .       (  Average 

13 

27 

23O 

410 

320 

73° 

290 

40 

Grains  of  applied  sulphate  of  (  Maximun 

1.34 

1-77 

5-25 

6.08 

6.83 

4.87 

6.90 

5.40 

alumina   per  gallon  of  ap-  -!  Minimum 

0.48 

0.75 

I.9I 

3.05 

2.80 

2.20 

2.19 

I.9I 

plied  water.         f  Average 

0.84 

1.17 

3-79 

3.61 

3-99 

3-7° 

3.66 

3-3^ 

Average  grains  of  applied  sulphate  of  alu 

mina  per  gallon  of  net  filtered  water  .  . 

0.89 

1.25 

4.26 

4.31 

4.87 

4.69 

4.21 

3-S7 

Degree  of   clearness  of  fil-      J  ^.'  '  . 
tercd  water..  .                     .  .  1  '  , 

2 
I 

4 

I 

5 

2 

2 
2 

3 
i 

3 
i 

4 
I 

3 
i 

••••••            (  Average 

,  .           .  .       .       (  Maximun 
Bacteria  per  cubic  centimeter  J  -,     . 

1.4 

3°7 
1  06 

2.5 

9  200 

2  COO 

3-3 
27700 
I  8()0 

2.O 

10  300 

Soo 

2.O 

8  1  ooo 

IO  f)OO 

2.O 

55  ooo 
14400 

2.  2 
21  SOO 
4  IOO 

1-9 
44  ooo 
4500 

in  liver  water  '}  Average 

168 

4  7oo 

IO  IOO 

4  600 

34  400 

33  800 

1  6  ooo 

17  900 

Average  maximum  number  of  bacteria  pe 

cubic  centimeter  in  filtered  water  

96 

479 

559 

84 

474 

432 

238 

365 

Average  minimum  number  of  bacteria  pe 

- 

cubic  centimeter  in  filtered  water  

20 

183 

157 

46 

136 

252 

55 

59 

I  Maximum 
Bacteria   per  cubic  centimeter  \  Mi,limum 

in  filtered  water.     .            .  .   )   , 

99 

12 

So 

928 

IO 

127 

25 

57" 
54 

534 

238 

219 

735 
29 

(  Average 

42 

349 

328 

72 

290 

350 

121 

224 

(  Maximun 

91.7 

98.2 

99.9 

99.2 

99.8 

99-4 

99-7 

99.8 

Average  Bacterial  efficiency...  •<  Minimum 

60.9 

86.  2 

91.3 

94.2 

96.9 

98.3 

98.5 

95-0 

(  Average 

75-0 

92.6 

96.8 

98.4 

99-1 

99.0 

99-2 

98.8 

SUMMARY  AND   DISCUSSION   OF  DATA    OF   1895-96. 


233 


NO.  4. 

RESULTS  BY  PERIODS. 

System. 


9 

10 

11 

12 

13 

14 

15 

16 

17 

18 

19 

20 

Mar.  20 

Mar.  23 

Mar.  30 

Apr.  7 

Apr.  27 

May  18 

May  28 

Junes 

June  9 

June  30 

July  6 

July  21 

9.00  A.M. 

9.  30  A.M. 

4.23  P.M. 

12.  37  P.M. 

g.OOA.M. 

II.I4A.M. 

2.17  P.M. 

3-30  P.M. 

9-34  A.M. 

3.48  P.M. 

2.21  P.M. 

4.41  P.M. 

Mar.  23 

Mar.  30 

Apr.  7 

Apr.  27 

May  18 

May  28 

June  3 

June  g 

June  30 

July  6 

July  21 

July  31 

9.  30  A.M. 

4.23  P.M. 

12.37  P.M. 

g.OOA.M. 

11.14  A.M. 

2.17  P.M. 

3-  30  P.M. 

9-  34  A.M. 

3  48  P.M. 

2.21  P.M. 

4.41  P.M. 

g.ooA.M. 

136-141 

142-178 

179-195 

196-205 

206-240 

241-253 

254-275 

276-284 

285-302 

303-310 

311-329 

330-346 

;.-  - 

5.60 

8.32 

1  1.  80 

15-38 

21.40 

11.23 

10.88 

10  32 

5-23 

7.63 

7-25 

2.48 

2.42 

2.30 

2.13 

7-45 

9.20 

2.08 

5.92 

4-43 

2.30 

3-73 

1.22 

2.92 

4.02 

3-95 

8.57 

11.27 

15.15 

4-47 

7.91 

6.77 

3-33 

5.46 

3  71 

2-77 

5-28 

8.00 

11.40 

14.92 

20.90 

10.67 

10.40 

9.87 

4.80 

7.22 

6.90 

1.98 

2.08 

2.03 

1.83 

6.88 

8.78 

1.67 

5.52 

4.07 

1.48 

3-33 

0.65 

2-53 

3-7" 

3.65 

8.20 

10.80 

14.67 

3-97 

7-43 

6.34 

2.90 

5.08 

3.28 

0.50 

o.55 

o.35 

0.47 

0.68 

o.  60 

o.  60 

0.58 

0.62 

0.57 

0.47 

0.55 

0.30 

0.25 

0.27 

0.28 

0-35 

0-35 

0.35 

0.40 

0-33 

o-37 

0.33 

0-35 

"•37 

0.32 

'  0.30 

o.37 

0.47 

0.48 

0.50 

0.48 

0.43 

0.43 

0.38 

0-43 

3426 

5889 

8515 

15  366 

18  164 

21  296 

12  607 

10  865 

13  326 

6496 

10629 

9273 

2569 

2  256 

2  266 

2  IlS 

S  240 

IO060 

2085 

7  154 

5  5i8 

2337 

4451 

I  471 

2991 

4  112 

4016 

10015 

13394 

16044 

5049 

8737 

8617 

4188 

6876 

3981 

3248 

5  74° 

8086 

15378 

18  283 

20485 

12  786 

10927 

13473 

6  594 

9826 

9382 

2  129 

2  O28 

2  117 

I  959 

8343 

8622 

2  131 

7292 

5549 

2  030 

4500 

6l7 

2737 

3952 

3857 

10016 

13485 

15540 

4672 

8726 

8  590 

3966 

6890 

3871 

517 

556 

521 

650 

I  073 

1389 

884 

728 

683 

670 

646 

878 

429 

353 

4OO 

421 

4f'3 

611 

557 

617 

506 

473 

515 

424 

468 

440 

450 

5i8 

684 

985 

707 

672 

569 

5f>3 

572 

622 

0 

0 

0 

o 

0 

0 

o 

o 

o 

o 

o 

O 

o 

o 

O 

o 

o 

0 

o 

o 

0 

b 

o 

o 

0 

0 

0 

o 

0 

0 

0 

0 

0 

o 

o 

o 

-131 

228 

430 

176 

404 

150 

298 

44 

61 

386 

44 

412 

158 

167 

158 

44 

35 

44 

35 

44 

35 

44 

26 

44 

239 

177 

189 

118 

61 

70 

68 

44 

44 

127 

43 

158 

37 

28 

27 

28 

it 

9 

33 

10 

II 

41 

'   15 

79 

18 

II 

8 

4 

4 

4 

6 

6 

4 

10 

6 

8 

24 

15 

1  6 

6 

6 

7 

1  6 

8 

7 

17 

9 

19 

19.5 

18.9 

18.4 

25.0 

21.8 

19.7 

23.2 

22.7 

23.0 

23-3 

23-3 

23.1 

17-3 

16.2 

1  6.  8 

17.4 

19.7 

16.1 

15.6 

16.4 

21.  0 

22.2 

22.1 

13-1 

17.9 

17.8 

17.6 

20.  6 

20.8 

17-7 

19.7 

19.6 

22.6 

22-7 

22.6 

19.7' 

118 

"4 

in 

152 

132 

119 

141 

137 

140 

142 

142 

141 

105 

98 

102 

105 

119 

98 

95 

99 

127 

134 

134 

So 

108 

108 

107 

125 

126 

107 

119 

119 

137 

137 

137 

119 

13.0 

12.7 

14.2 

18.3 

18.5 

17.1 

15.9 

16.9 

19.7 

17-4 

ig.I 

14-3 

79 

77 

86 

ill 

112 

104 

96 

102 

119 

105 

116 

87 

12 

22 

33 

61 

73 

84 

49 

43 

53 

24 

34 

35 

6 

7 

7 

6 

31 

35 

6 

27 

20 

7 

16 

5 

10 

15 

M 

39 

52 

52 

18 

31 

33 

15 

26 

13 

I  276 

660 

I  131 

370 

1  80 

200 

829 

459 

582 

1674 

637 

3347 

993 

338 

400 

70 

57 

38 

540 

1  60 

210 

720 

190 

i  050 

I  130 

450 

800 

1  80 

100 

90 

680 

290 

295 

I  090 

440 

i  740 

6.60 

9.08 

6.72 

1.92 

2.68 

1.  80 

5.90 

5-33 

4.67 

6.07 

5-75 

9.62 

5-21 

2.78 

3-25 

o.73 

0.49 

0.83 

3.16 

2.32 

I.IO 

3-37 

2.29 

3-36 

5.97 

4-43 

5.<>7 

1.33 

1.41 

1-33 

4-52 

4.03 

2.64 

4.61 

3.02 

6.27 

7.85 

5-22 

6.03 

1.42 

1.50 

1.43 

5.50 

4.38 

2.84 

5-55 

3-32 

7-75 

2 

5 

3 

3 

3 

2 

2 

2 

2 

3 

4 

5 

2 

2 

2 

I 

I 

I 

2 

I 

I 

i 

2 

2 

2.0 

2.8 

2.6 

2.O 

2.1 

1.6 

2.0 

i-7 

1-7 

2.O 

2.2 

3-1 

60  100 

55400 

42700 

17  800 

7400 

10  500 

28  700 

14000 

13900 

24  2OO 

17  loo 

34  too 

41  6OO 

25  700 

19  200 

4OOO 

3  700 

i  500 

8  200 

4  900 

6  500 

9500 

5500 

9500 

54600 

40300 

27700 

9500 

5  600 

4500 

20  IOO 

8600 

9500 

15  ooo 

8  900 

22  IOO 

3OQ 

211 

203 

165 

140 

112 

55 

163 

8g 

604 

I'>4 

78 

III 

62 

73 

29 

23 

45 

3<> 

225 

329 

245 

635 

295 

i  075 

116 

293 

87 

298 

105 

95 

i  475 

93 

5" 

35 

23 

ii 

32 

40 

22 

20 

4<) 

17 

13 

181 

120 

M5 

113 

137 

57 

I  Of. 

4° 

1  06 

70 

47 

354 

99.8 

99.9 

99-8 

99.8 

99.8 

99.4 

99.8 

998 

99-7 

99-7 

99.8 

99-9 

99.4 

95-4 

99-7 

96.3 

85.5 

97-4 

98.7 

99.8 

95-3 

99.0 

98.6 

94-7 

99-7 

99-7 

99-5 

98.8 

97-5 

98.7 

99-5 

99  '5 

98.9 

99-5 

99-5 

98.4 

234 


WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE  No 

SUMMARIES   OF   RESULTS 
Jewel 


Number  of  period  

1 

2 

3 

4 

5 

6 

7 

8 

Feb.  29 

(  Date 
Jieean.    .                                 .  .    -<  ,T 

3ct.2i,'95 

Nov.  21  j  Dec.  24 

an.  13,  '96 

Jan.  25 

Feb.  6 

Feb.  ii 

j  I  lour 

2.  03  P.M. 

i.  38  A.M.:  1.36  P.M.  9.44A.M. 

2.00  P.M. 

2.33  P.M. 

)  45A.M.  9.58  A.M. 

Ended  .  .                                   .  .  *  P^te 

Vov.21/95 

Dec.  24   Jan.  13,  '96    Jan.  25 

Feb.  6 

Feb.  ii      Feb.  29     Mar.  20 

/  Hour 

[1.38  A.M. 

1.36  P.M. 

9.44  A.M. 

2.00  P.M. 

2.33  P.M. 

9.45  A.M.  9-58  A.M.  19.37  A.M. 

Runs  included  in  period          

I—  12 

13—20 

21-29 

30—34 

35-39 

40-42 

43-52 

53-64 

I  Maximum 

21.  IO 

28.83 

16.30 

23-55 

14-58 

9-63 

20  55 

24.17 

Period  of  operation.    (Hours.)  •;  Minimum 

5-20 

16.60 

6-97 

16.08 

8-55 

8.33 

7-95 

6-73 

(  Average 

I3-I7 

21-97 

11.00           18.80 

II-35 

9.02 

13-52 

11.84 

(  Maximum 

20.78 

26.10 

15-65 

23.12 

14.23 

9-35 

20.07 

23.80 

Period  of  service.    (Hours.).  .  -J  Minimum 

4.85 

15-93 

6.57 

15-57 

8.22 

7.80 

7-45 

6.30 

(  Average 

12.82 

21.40 

10.38 

18.38 

10.87 

8.45 

12-95 

11-54 

(  Maximum 

O.5O 

0-95 

1.03 

o  52 

0.83 

0.87 

0.83 

0.43 

Period  of  wash.   (Hours.).  •  •  •  i  Minimum 

0.27 

o-33 

o  37 

0.32 

0-33 

0.28 

0.37 

0.25 

(  Average 

0-35 

o  57 

0.62 

0.42 

0.48 

0.57 

0.57 

0.30 

Quantity  of  applied  water.        j  Minimum 
(Cubic  feet.  )..                           1   . 

36355 
7896 
19  889 

40391 
21  730 
30524 

21  089 

7932 
13673 

354io 

22  289 
26  464 

2O  6O7 
II  074 
15299 

13  280 
10  225 
ii  509 

22  575 
10  224 
16  523 

35421 
8  790 
17404 

(  Average 

Quantity  of  filtered  water.         i  ;*lximum 
(Cubic  feet.)...  . 

34677 
7781 
19363 

38352 
20488 
29  701 

21  335 
7947 
13643 

34946 
22  351 
26442 

20433 
I07I5 
15  O62 

13  127 

IO  220 
II  319 

22  950 
10237 
16770 

35292 
8  840 
17634 

(  Average 

Quantity  of  wash  water.              Maximum 
1  (Cubic  feet)  j  Minimum 

731 
259 
519 

856 
534 
676 

i  025 

467 
665 

45S 
432 

443 

617 

383 

447 

538 

49° 
517 

810 
505 
579 

844 
442 
559 

(  Average 

...        /•  m        i                       i  Maximum 
Quantity  <>i  filtered  waste          \  ,,.    . 
v                 .,,   ,  .    ,    .                 J.  Minimum 
water.     (Cubic  feet  )  .  . 

0 
0 

o 
o 

443 
o 

301 
o 

310 

9 

403 

0 

308 

0 

97 
o 

(  Average 

o 

o 

122 

60 

136 

134 

66 

8 

Quantity  of  unfiltered  waste      \  ,,'.  x. 
,r>  i  •     c    L  \               •{  Minimum 
water.    (Cubic  teet.)  )   . 
(  Average 

235 
32 
104 

214 

32 

IOO 

32 
32 
32 

32 
32 
32 

32 
32 
32 

32 
32 
32 

32 
32 

214 

0 

31 

Percentage  which  wash  and      j  Maximum 

8 

3 

II 

4 

9 

9 

7 

IO 

waste  water  was  of  applied  -1  Minimum 

2 

2 

3 

i 

2 

4 

2 

2 

water  (  Average 

3 

3 

ft 

2 

4 

6 

4 

3 

(I  Maximum 

27.8 

24.5     i        23.1 

25.2 

24.0 

23-4 

29.0 

30.1 

Cubic  feet  per  min.  -!  Minimum 

22.9 

21.5             20.  i 

23.4                21.2 

21.5 

14.0 

23-4 

(  Average 

25-3 

23.1             21.9 

24.0                23.1 

23-3 

21.6 

25.5 

.,.,        ,             -  -   .  (  Maximum 

112 

99                93 

I  O2 

97 

95 

118 

122 

L-<  Minimum 

93 

87 

Si 

95 

86 

87 

57 

95 

i       per  24  hours.  .  . 
(  Average 

102 

93 

89 

97                93 

94 

87 

103 

Ave.  net  rate  (  Cubic  feet  per  minute  

24.4 

22.5 

19-5 

24.1 

21.6 

22.5 

19.6 

24.5 

of  filtration  j  Mil.  gals,  per  acre  per  24  hr. 

99 

91 

79 

97               87 

91 

79 

99 

Net  quantity  of  filtered  waste  j  M-'X 
^per  run,  mil.  gals,  per  acrel   .  "'" 

99 

20 

54 

105 
59 

82 

57 
20 
36 

97 
60 

73 

56 
28 
41 

35 
27 
30 

62 
27 
44 

96 

22 

47 

Average  estimated  suspended  (  Maximum 

25 

35 

850 

60     :         460 

970 

430 

2IO 

solids  in  river  water.    (Parts  -|  Minimum 

7 

15 

80 

20             250 

580 

120 

50 

per  million)  .  /  Average 

16 

26 

345 

35              320 

730              290 

70 

drains   of    applied    sulphate  (  Maximum 

2  41 

1.26 

4.42 

1.  12             2.32 

2.39             4-82 

1-55 

of    alumina    per    gallon    of-]  Minimum 

0.40 

0.48 

1-25 

0.83             i.  21 

2.16 

1.36 

0.65 

applied  water     f  Average 

O.6S 

0.87 

2.35 

0.96             1.72 

2.25 

2.78 

i.  06 

Average    grains   of  applied    sulphate   of 

alumina  per  gallon  of  net  filtered  water. 

0.70 

0.90 

2.50 

0.98             1.80 

2.40             2.90 

i.  ii 

Degree  of  clearness  of  filtered  (  Ma««m™ 
water.                                     ]  Minimum 

3 
i 
1.6 

3 
i 
1.6 

5 

2 
3-2 

3                   5 

2                         2 

2.6                3.7 

4 

2 

3-0 

5 
2 
2.9 

5 

2 

(  Average 

Bacteria  per  cubic  centimeter  (  Maximum 
in  river  water  j  Minimum 

675 
126 

S  700 

2  IOO 

4400 

27  6OO 
I  8OO 
9700 

6  800         54  loo 
i  300         10  900 
3  800         22  900 

41  200 
14400 
33  loo 

21  800 
4700 
15  6OO 

34400 
9400 

1  8  500 

(  Average 

Average  maximum  number  of  bacteria  pei 

cubic  centimeter  in  filtered  water  

473 

611 

550 

315           i  779 

i  446 

2002 

779 

Average  minimum  number  of  bacteria  pci 

cubic  centimeter  in  filtered  water  

56 

115 

162 

105 

912 

418 

245 

124 

Bacteria  per  cubic  centimeter  (  Maximum 
in  filtered  water.  .  .                1  Minimum 

367 
26 
154 

659 

77 
271 

546 

202 
297 

248 
i  (.4 
186 

2372 

688 
1088 

i  346 
740 
960 

I  600 
504 
I  015 

1645 

35 
533 

(  Average 

83.1 

97-3 

98.2 

96.3 

98.0 

98  i 

97-4 

99-6 

Average  bacterial  efficiency.  .  •<  Minimum 

o.o 

83-5 

88.8 

86.4 

86.0 

94-9 

90.6 

94-7 

(  Average 

59-o 

93-8 

96.9 

95.1 

95-3 

97-1 

93  5 

97-1 

SUMMARY  AND  DISCUSSION  OF  DATA   OF   1895-96. 


235 


4. — Continued. 
BY  PERIODS. 
System. 


9 

10 

11 

12 

13 

14 

15 

16 

17 

18      19 

20 

Mar.  20 

Mar.  21 

Mar.  30 

Apr.  7 

Apr.  27 

May  18 

May  28 

June  3  i  June  9 

July  i   July  6 

July  22 

9-37  A.M. 

5.08  P.M. 

10.  30A.M. 

9.23  A.M.  9.25  A.M. 

1.  12  P.M. 

II.O5  A.M. 

2.20  P.M.  10.56  A.M. 

3-55  P.M.  2.20  P.M. 

I0.24A.M. 

Mar.  21 

Mar.  30 

Apr.  7 

Apr.  27  May  18 

May  28 

June  3 

June  9    July  I 

July  6  i  July  22 

July  30 

5.08  P.M. 

10.30  A.M. 

9.23  A.M. 

9.25  A.M. 

1.  12  P.M.  II.O5  A.M. 

2.20  P.M. 

10-56  A.M.  3.55  P.M. 

2.20  P.M.  10.24  A.M. 

11.37  A.M. 

65-69 

70-96 

97-1  1  1 

112-125 

126-148!  149-158 

159-184 

185-204 

205-234 

235-238 

239-256 

257-272 

3-5S 

8.83 

6.  02 

16.92 

21.00 

34-77 

8.55 

8.68 

13.68 

7-OO      8.97 

8.52 

2-73 

3-17 

1.08 

3-90 

5-57 

13-77 

0-93 

1.  08 

1-43 

1.85 

1.98 

0.72 

3.20 

5.65 

3.86 

9-79 

16.90 

21.63 

2.65 

3-55 

5.02 

4.25 

5.55 

3.48 

3-i8 

8.53 

5-77 

16.62 

20.70 

34-48 

8.30 

8.45 

13.15 

6.50 

8.57 

7.98 

2.38 

2.63 

0.15 

3-67 

5-40 

13-50 

0.63 

0.82 

i.iS 

1-43 

1.28 

0.52 

2.85 

5-35 

3-53 

9.52 

16.62 

21-35 

2-43 

3.30 

4.70 

3.85 

5-13 

3.10 

0.43 

0.70 

0.93 

0.32 

0.48 

0-35 

0.30 

0.35     0.77 

0.50 

0.38 

0.60 

0.27 

0.18 

0.23 

0.20 

0.17 

O.2O 

0.17 

0.20 

o.  20 

0.23 

0.27 

o.  20 

o.35 

0.30 

o-33 

0.27 

0.28 

0.28 

0.22 

0.25       0.32 

0.40 

0.42 

0.38 

4437 

12  iSl 

7814 

23  g«2 

3I3I9 

51  286 

12  533 

12540   1  18448 

9046 

12  274 

12274 

3288 

3903 

776 

5158 

8623 

21  OI2 

I  032 

2  637   j   2  380 

2  062 

2  316 

858 

3948 

7427 

5050 

13641 

25  565 

33604 

4  220 

5627      7120 

5553 

7699 

4024 

4434 

12513 

8015 

24483 

32  264 

51483 

12  229 

12  463 

17699 

8971 

12396 

9903 

3350 

3770 

183 

5286 

8817 

20795 

I  041 

I  806 

2  Ogl 

i  860 

i  888 

855 

3989 

7659 

5094 

13927 

26  225 

34174 

3904 

5  443 

7  it>5 

5360 

7497 

4038 

625 

617 

745 

1073 

874 

732 

799 

Soi 

i  996 

i  443 

i  105 

I  078 

469 

395 

464 

427 

.  398 

508 

469 

486 

515 

958 

582 

376 

555 

5'0 

598 

636 

580 

606 

59' 

587 

756 

i  151 

860 

772 

12 

245 

592 

0 

176 

93 

206 

107 

763 

81 

417 

H3 

O 

o 

o 

o 

o 

0 

o 

o 

0 

0 

0 

0 

2 

17 

75 

o 

9 

12 

15 

19 

78 

43 

73 

10 

114 

0 

0 

274 

0 

O 

0 

0 

214 

0 

187 

198 

O 

o 

o 

o 

o 

0 

o 

o 

0 

0 

o 

0 

23 

0 

o 

15 

o 

0 

o 

0 

7 

o 

20 

37 

18 

22 

142 

8 

6 

3 

47 

20 

3i 

51 

50 

63 

II 

5 

7 

3 

I 

I 

6 

5 

5 

16 

6 

10 

15 

7 

'3 

5 

2 

2 

15 

II 

12 

21 

12 

20 

23.8 

25.2 

24.9 

25.3 

27.2 

29.6 

34-5 

35-2 

37-0 

23.8 

25.0 

30.9 

22.6 

22.7 

20.3 

23.2 

25.1 

24.4 

20.5 

24.5 

22.4 

21.6 

23.1 

iS.a 

23.3 

23.8 

24.0 

24.4 

26.3 

26.7 

26.8 

27.5 

25.2 

23.2 

24.2 

21.8 

96 

102 

101 

102 

110 

1  2O 

140 

M3 

150 

96 

IOI 

126 

91 

92 

82 

94 

IOI 

99 

83 

99 

9i 

87 

93 

74 

94 

96 

97 

99 

1  06 

108 

108 

in 

102 

94 

98 

88 

17.5 

20.  2 

19.0 

22.2 

24.6 

25-4 

22.6 

23.5 

20.7 

17.1 

20.  i 

15-5 

71 

82 

77 

90 

too 

103 

91 

95 

84 

69 

81 

63 

105 

32 

20 

65 

86 

141 

32 

33 

45 

21 

3i 

24 

7 

8 

O 

13 

22 

57 

2 

5 

5 

3 

3 

I 

9 

19 

12 

36 

70 

9i 

10 

14 

17 

12 

19 

9 

I  280 

730 

I  130 

350 

igO 

130 

830 

460 

590 

I  700 

690 

3400 

990 

340 

490 

70 

60 

40 

400 

1  60 

1  80 

I  OOO 

190 

I  200 

I  130 

450 

850 

1  60 

IOO 

80 

640 

300 

340 

I  310 

450 

I  860 

5-40 

5-23 

6.32 

2.23 

3.66 

1.84 

6.92 

7.70 

7.61 

7-45 

7-17 

12.62 

2.88 

2-39 

3-1° 

0.96 

I-I3 

0.56 

1.46 

3-52 

1.29 

5-30 

4.26 

5.76 

4.17 

3-44 

4-36 

1-34 

1.76 

1.26 

4.76 

4.96 

4.29 

6.35 

5.65 

8.58 

4.91 

3-70 

5.02 

1.41 

1.  80 

1.29 

5.6o 

5.58 

5.00 

8.14 

6.58 

10.72 

3 

4 

3 

2 

2 

2        4 

2 

2 

3 

2 

3 

3 

2 

2 

I 

I 

I        I 

I 

I 

i 

I 

2 

3-o 

2.6 

2.6 

1.4 

1.2 

1.4       2.7 

1.8 

1-3 

i-7 

1.6 

1.2 

60  100 

53  ooo 

42  700 

I9OOO 

8300 

6  2OO 

32  500 

16  700 

18  ooo 

24  200 

17  100 

37300 

41  600 

25  900 

19400 

3  too 

3700 

I  800 

8  200 

4300 

6  ooo 

12  2OO 

5  100 

9500 

55300 

40  100 

cgr 

28  100 

8000 

5700 
684 

4300 

i«8 

19  300 

8  800 

9300 
219 

18  ooo 

98 

9300 

122 

22  IOO 

301 
244 

449 
264 

123 

27 

oc 

1  D° 
-j-i 

68 

29 

26 

1905 

I  250 

1495 

-  / 
I64 

*  J 
1  60 

Jj 
92 

475 

107 

655 

127 

409 

745 

440 

103 

32        8 

12 

38 

22 

7 

5 

4 

3 

6 

968 

4l6 

522       50 

48 

73 

IgO 

47 

9i 

43 

62 

86 

99-3 

99-7 

99-8 

99-8 

99-7 

98.8 

99.8 

99-9 

99-9 

99-9 

99.9 

99-9 

96.6 

97-7 

95.0 

98.2 

97.6 

94-9 

97.6 

98.9 

91.0 

99-5 

94-1 

97.8 

98-3 

99.0 

98.1 

99-4 

99.2 

98.3 

99.0 

99-5 

99-o 

99.8 

99  3 

99.6 

236 


WATER  PURIFICATION  AT  LOUISVILLE. 


TABLE 
SUMMARIES  OF 

Western  Gravity 

1 

2 

3 

4 

5                 6 

7 

8 

Beean                                         \  Date 

lee.  24,  '95  _ 

9.42A.M. 

fan.  14,  '96 

O.52  A.M. 

2-16 

23.13 
2.38 
8.C2 
22.75 

1.88 
7.70 
0.50 
0.17 
0.32 
13036 
I  564 
4544 
12  679 
982 
4267 
616 
162 
419 
242 
37 

101 

400 
5° 
169 
48 
5 
15 
II.  6 
7-9 
9.2 
72 
48 
57 
8.0 

49 
51 
4 
17 

870 
80 
290 

fan.  14,  '96 

IO.52  A.M. 

Jan.  27 
9.29  A.M. 
17-26 
13.93 
6.72 
8.37 
13.40 
6.42 
8.07 
0.53 

O.20 
O.3O 
II  766 

73" 
9969 
ii  534 
6989 
9632 
864 
350 
448 
215 
74 
129 
347 
o 
208 

12 

7 
8 
24.7 
11.4 
19.9 
152 
7° 
123 
18.3 
"3 
45 
28 
39 
50 
17 

27 

1.65 

Jan.  27 
9.29A.M. 
Feb.  7 
9.23  A.M. 

27-39 
7.90 
3-28 
4-95 
7.70 
2.98 
4.67 
0.32 

0.20 
0.28      : 
7098 
2305 
4058 
6982 
2  009 

3  7°5 
839 
269 
466 
'74 
40 
103 
600 
50 
250 
50 
7 

20 
I5.I 
10.7 
13.2 

94 
64 

8  1 

II.  0 

68 
28 
6 
M 
460 

320 
2.79 

Feb.  7 
9.23  A.M. 
Feb.  ii 
9.21  A.M. 

40-48 
3.83 
1.88 
2.82 
3-57 
1.62 
2.52 
0.40 
0.27 
0.30 
3375 
i  240 
2257 
2748 
95i 
i  805 
503 
256 
404 
227 
109 
151 
400 

100 

301 
66 
23 
38 
15.9 
5.8 
ii.  7 
98 
3" 
72 
8.3 
5i 
10 

2 

6 

970 

640 

780 

Feb.  ii 
9.21  A.M. 
Feb.  28 
12.12  P.M. 
49-80 
7.07 
0.50 
3-68 
6.80 
0.25 
3-43 
0.38 
0.17 
0.25 
6967 
258 
3  206 
6812 
79 
2  951 
620 
97 
425 
179 
3i 
104 
730 
o 
'54 
146 
9 
21 
19.2 
5-3 
14-4 
118 
33 
89 
ii.  5 
7i 
27 
o 
ii 
560 
no 

280 
9.33 
0.78 
1.94 

2.46 

3 
i 

1-5 

28  ooo 
4  100 
16  200 

652 

3" 
i  137 
69 
541 
99-5 
93-0 
96.7 

Feb.  28 
12.12  P.M. 
Mar.  20 
10.09  A.M. 
Si-ioo 
11.77 

2.4G 

7.30 
11.47 
2.23 
7.07 

0.32 
o.iS 
0.23 
13798 

2  552 

8  502 
13  500 
2087 
8236 
613 
402 
527 

2lS 
41 
98 
42O 
70 

178 
42 
5 
9 
20.3 
13.9 
19-5 
126 
85 
J2I 
17-7 
109 
56 
6 
33 

210 
40 
67 
1.42 
0.59 
0.78 

0.86 

2 
I 

1-5 

39700 
7700 

22  OOO 

735 

285 
1941 
140 
520 
98.9 
95-1 
97.6 

'  '  (  Hour 
Knded                                               i  Date 

led  \  Hour 
Runs  included  in  period  

(  Maximum 
Period  of  operation.    (Hours.  )•<  Minimum 

(  Average 
Maximum 

(  Average 

Period  of  wash.      (Hours.).  .  .  -!  Minimum 
(  Average 

Quantity  of  applied  water.        j  ^^™ 
(Cubic  feet.)  1  * 

Quantity  of  filtered  water.         (  JJ^™™ 
(Cubic  feet.)  ...                   .  .  )   . 

Quantity  of  wash  water.             (  w™"™™ 

(Cubic  feet.)  (Average 

Quantity   of  filtered   waste      (  M^ni'mum 
water.      (Cubic  feet.  )  |  Average 

Quantity  of  unfiltered  waste      \  Maximum 

w.iter.     (Cubic  feet.)  }  Average 
Percentage  which  wash  and      (  Maximum 
waste  water  was  of  applied  -|  Minimum 

["                                       (  Maximum 
Actual          Cubic  feet  per  min.  •<  Minimum 
rate  of                                          (  Average 
filtra-          ,-.,                               (  Maximum 

£   "ysar  >F™ 

(  Average 
Ave.  net  rate  (  Cubic  feet  per  minute  
of  filtration,  j  Mil.  gals,  per  acre  per  24  hr 
Net  quantity  of  filtered  waste  j  Maximum 
per   run,    in   mil.   gals,    per-!  Minimum 

Average  estimated  suspended  I  Maximum 
solids  in  river  water.  (Parts  -1  Minimum 
per  million.)  (  Average 

Grains  of  applied  sulphate  of   (  Maximum 
alumina   per  gallon  of  ap-  -!  Minimum 
plied  water  (  Average 

2.67 

3.14 
3 
i 

i-7 
32  400 
i  800 
8  200 

396 

214 
7S3 
81 
302 
98.8 
93-2 
96-3 

1.07 
1.16 

2 
I 
1.6 
7  300 
i  900 
4  800 

195 

-   98 
228 
68 
148 
98.6 
92.6 
96.9 

1.86 

3-32 
4 

I 

2.2 
8l  OOO 
12000 

37  600 

880 

386 
1586 
127 
679 
99.0 
92.7 
98.2 

3.22 

5.20 

3 
i 

55  ooo 
14400 
34500 

Average  grains  of  applied  sulphate  of  alu 
mina  per  gallon  of  net  filtered  water  .  .  . 

Degree   of  clearness   of   fil-     {  Ca 

tered  water  (Average 
Bacteria   per  cubic  centimeter  (M-imum 

Average  maximum  number  of  bacteria  per 
cubic  centimeter  in  filtered  water  

Average  minimum  number  of  bacteria  pci 

Bacteria  per  cubic  centimeter  (  J5i™m 
in  filtered  water  (Average 
(Maximum 
Average   >acterial  efficiency.  .  •)  Minimum 
(  Average 

i  600 
252 
679 
99-3 
95-9 
98.0 

SUMMARY  AND   DISCUSSION   OF  DATA    OF   1895-96. 


237 


No.  4. — Continued. 
RESULTS   BY    PERIODS. 
System. 


9     i 

10 

11 

12 

13 

14 

15 

16 

17 

18 

19 

20 

July  2 

July  10 

July  24 

9.37  A.M. 

9.32  A.M. 

10.55  A.M. 

July    2 

July  10 

July  24 

July  31 

9.32  A.M. 

10.55  A.M. 

5.17  P.M. 

107-114 

115-120 

I2I-I23 

4.48 

8.12 

6.23 

O.78 

1.25 

1.78 

1.25 

2.05 

4.70 

3-75 

3-97 

7-37 

3.30 

o  53 

0.80 

1.13 

I.OI 

'•57 

4.08 

2.53 

o  58 

0.60 

0.75 

2.73 

0.17 

0.40 

0.43 

0.23 

0.28 

0.48 

0.62 

1.22 

i  133 

3  537 

7023 

4788 

616 

935 

i  248 

I  014 

996 

I  564 

4067 

2  920 

i  081 

3  253 

6  753 

2981 

280 

613 

i  005 

715 

580 

I  262 

3  76° 

2  O27 

784 

892 

93° 

1298 

47° 

727 

631 

<68 

60  1 

806 

901 

322 

360 

393 

I  672 

179 

196 

61 

261 

284 

688 

660 

100 

240 

240 

40 

0 

0 

130 

287 

52 

102 

200 

93 

5° 

91 

33 

10 

46 

58 

29 

6  1 

14.1 

'5-7 

14.2 

8  8 

12.8 

14.8 

ii.7 

12  5 

13.5 

15.3 

13.3 

89 

IOI 

91 

83 

96 

75 

87 

86 

i  6 

5  3 

IO.  2 

5.1 

65 

26 

8 

6 

6 

640 

J 

5  89 

5  J8 

, 

8  58 

169 

71 

216 

511 

7  16 

ft? 

08  1 

98  6 

98  9 

1 

WATER   PURIFICATION   AT  LOUISVILLE. 


TABLE  No. 

SUMMARIES     OF 
Western     Pressure 


1 

2 

3 

4 

5 

6 

7 

8 

(  Date 

Dej.23,'95 
I0.35A.M 
an.  14,  '96 

11.03  A.M 
I  -10 

32.72 
6-55 
12  02 
32.38 
6.13 
11.67 
0.42 
0.22 
0.35 
43978 

6  006 
13  690 
43  793 
(>  7-15 
13  550 
760 
493 
653 
185 
Si 
'43 
o 
o 
o 

12 
2 

6 

22.5 

14.8 

io-4 
1  60 
105 
138 
17.9 
127 
209 
32 
62 
870 

100 

320 

Jan.  14,  '96 

I  I  .  O3  A  .  M  . 

Jan.  27 
3  51  I'-M. 
11-14 

28.47 
18.55 
22.92 
28.08 
18.25 

22.51 

0.55 
0.30 
0.38 
47  172 
31  213 
35382 
4"939 
31  M7 
35  156 
6Si 
638 
663 
309 
176 
225 
o 

0 

o 
3 
2 

28.4 
22.3 
27.8 
2O2 
I5S 
197 
25.2 
I78 
225 
142 
168 

TOO 
20 

42 

I  37 
0.87 
i.  06 

i.  08 
2 
I 
I.I 

7  ooo 

2  300 

4  800 
421 

82 
322 
116 
206 
96.8 
95-o 
95-7 

Jan.  27 
3.51  P.M. 
Feb.  7. 

9.32  A   M. 

15-21 

8.73 
7.25 
S.oo 
8.27 
6.97 
7.63 
047 
0.28 
0-37 
II  660 
7656 
9  609 
1  1  479 
7431 
9395 
790 

471 
626 
.280 
166 
214 
o 
o 
o 

12 

7 
9 
24.0 
16.4 
20.5 
170 
"5 
146 
18.3 
130 
53 
33 
42 
464 
244 
340 
2.64 

1-39 
2.04 

2.24 
5 
i 
2.4 
71  ooo 

12  4OO 
39000 

I  087 

428 
I  461 

188 
760 
99.1 
93.2 
98.1 

Feb.  7 

9.32  A.M. 

Feb.  II 

11.32  A.M 

22-27 
8.27 
2.72 
4-35 

7-97 
2-55 
4.07 
0.32 
0.27 
0.28 
9  722 
3  263 
5  128 
9536 
3081 
4938 
662 
431 
520 
269 
Mi 
190 
o 
o 
o 

21 

9 

14 
26.5 
18.4 

20.2 

188 

131 
143 
16.9 

119 

43 
13 

21 

967 
636 
750 
3.08 
0.71 
3.22 

3-75 
3 
i 
2.0 
55  ooo 
14400 
32  500 

i  027 

459 
967 
166 
68  1 
98.9 
95-8 
97-9 

Feb.  II 
11.32  A.M. 
Feb.  27 

2.10  P.M. 

28-44 

13.12 

3.23 

6-55 
12.78 
3.02 
6.25 
0.38 

0.22 
0.30 
17997 
3896 
8368 
17819 

3739 
8  219 

832 
375 
602 
271 
63 

149 
o 

0 

o 

17 

5 
9 
23-5 
19.9 
21.9 
1  66 
141 
155 
19.4 
138 
S3 
16 
39 
500 
126 
290 
4-23 
i.  06 
2.25 

2.48 

5 
i 

2-4 

28000 
10  700 
16  600 

829 

257 
975 
151 
544 
99-2 
9i-3 
96.7 

Feb.  27 

2.IOT.M. 

Mar.  20 
9.  20  A.M. 
45-52 
25.42 
8.50 
19.40 
25-17 
S.oo 
19.05 
0.50 
0.25 
o.35 
35056 
10445 
26859 
34825 

10  001 

26  642 

898 
606 

749 
444 

101 

218 
o 
o 

0 
12 
2 
4 
24.2 
20.8 
23-3 
171 
148 
I65 
22.2 

157 
166 
44 
125 

210 
40 
70 

•    1-44 
0.69 
0.84 

0.86 

3 
i 
1.8 
37  500 
8  700 
17  800 

i  549 

221 
I  382 

233 
556 
98.2 
91.8 
96.9 

i  Date 

1  Hour 

(  Maximum 
Period  of  operation.     (Hours.  )  -j  Minimum 
(  Average 
j  Maximum 
Period  of  seivice.     (Hours.).  .  )  Minimum 
(  Average 
{  Maximum 

Period  of  wa-h.     (Hours  )..    /Minimum 

(  Average 
Quantity    of    applied     water,  j  ^~ 

(  Average 

Quantity    of    filtered     water.    \  M'.lximum 
,f-*<    i  •     c     j.  \                                   \  Minimum 
(Cubic  feet.)  )   .Uvn«- 

Quantity     of    wash    water.        ),,."• 
(Cubic  feet  ) 

(  Average 

Quantity    of    filtered    waste        :  J 
water.     (Cubic  feet.).  ..       ,  j  Minimum 

(  Average 

r         ni.                   .     (  Maximum 
Quantity   of    unaltered   waste),..   . 

water      (Cubic   feet  ) 

'  (  Average 
Percentage   which    wash    and  (  Maximum 
•     waste  water  was  of  applied  -j  Minimum 

f                                     1  Maximum 
Actual       !  Cubic  feet  per  min.  •!  Minimum 
rate  of!                                         (Average 
f.ltra-     |  Mil.  gals,  per  acre  (  ^iximum 

tlon               per  24  hours....  i"mmlum 
(_      '                               (  Average 

of  nitration    j  Mil.  gals  per  acre  per  24  hr. 
re,.                 .     (  Maximum 
Net   quantity  of  filtered  waste  W,inimum 
per  run,  in  mil.  gals,  per  acre  |  Avenl  e 

solids  in  river  water.    (Parts  •]  Minimum 

Grains     of    applied    sulphate  f  Maximum 
of  alumina    per    gallon    of  •!  Minimum 

2.67 

2.84 

2 

I 

1.6 
35  700 
i  800 
9  200 

459 

183 
i  032 
107 
287 
98.8 
93-9 
96.9 

Average  grains  of  applied  sulphate  of  alu- 

Degree  of  c.earness  of  filtered  \*g~ 

(  Average 

,  .                          (  Maximum 
Bacteria  per  cubic  centimeter]  Minimum 

(  Average 
Average  maximum  number  of  bacteria  per 

Average  minimum  'number  of  bacteria  per 

,  .                          (  Maximum 
Bacteria  per  cubic  centimeter  (  Mimmum 

in  river  water  |  Average 

1  Maximum 
Average  bacterial  efficiency.  .  .  •<  Minimum 

(  Average 

SUMMARY  AND  DISCUSSION  OF  DATA    OF   1895-96. 


239 


4. — Concluded. 
RESULTS     BY     PERIODS. 
S  y  s  te  m. 


9 

10 

11 

12 

13 

14 

May  18 
9.15  A.M. 
May  28 
12.  18  P.M. 
108-112 
54.62 
20.87 
39-97 
54.67 
20.63 
39-65 
o.53 
0.23 
0.32 
45  180 
21  446 
35407 
45752 

21  786 

35  563 
783 
630 
671 
329 
107 
165 
o 
o 

0 

4 
2 
2 
17-6 
14.0 
14.9 
125 
99 
1  06 
14.5 
102 
215 
104 
1  68 
150 
50 
90 
1.87 
0.51 
1  .16 

i.ig 

3 
I 
2.0 
6800 
2  5OO 
3900 

875 

44 
5" 
75 
195 
gS-3 
90.5 
95.0 

15 

16 

17 

18 

19 

20 

Mar.  20 
9.20  A.M. 
Mar.  23 
9.19  A.M. 

53-57 
4-65 
2.08 
3.28 
4-33 
1-75 
2-95 
0.40 
0.25 
0.33 
3787 
2  276 

3  069 
3  595 
2043 
2873 
763 
625 
696 
294 
128 
196 
o 

0 

o 

44 
22 
29 
19.4 
13.5 
16.2 
137 
96 
"4 
II.  I 

79 
14 

6 
II 

I  276 
993 
I  140 

Mar.  23 
9.19  A  M. 
Mar.  30 
9.  ia  A.M. 

58-82 
9.03 
3-33 
5-95 
S.73 
3.00 
5.67 
o.33 

0.20 

0.28 

8797 
3230 

5566 

8907 
3070 

5  577 
962 
625 
737 
193 
58 
124 
o 

0 

o 

31 

IO 

15 

19.2 

14.6 
16.4 

136 
103 
n5 
'3-3 
94 
38 
1  1 
23 
660 
333 
450 
4.96 

I  of) 

Mar.  30 
9.14  A.M. 
May  7 
9.00  A.M. 

83-94 
8.52 
3-28 
5-55 
8.27 
2.93 
5-27 
0.38 
0.23 
0.28 
8746 
2307 
5025 
8875 

2  O62 

5  oio 
764 
656 
706 
245 
86 
156 

0 

o 
o 

40 

9 
17 
18.5 
11.7 
15.9 
132 
83 

112 
12.5 

88 
38 
7 
20 
I  131 
352 
780 
5.I6 

May  7 
g.oo  A.M. 
May  18 
9.15  A.M. 
95-107 
22.58 
1  1  .  go 
13-94 
22.37 
1  1.  60 
13.62 
o  40 

0.22 
O.32 
3M94 
16048 
19  223 
3IS07 
16053 

18  883 

79' 
481 
657 
270 
68 
168 
o 
o 
o 
6 
3 
4 
24.2 
22.1 
23.1 
I?' 
'57 

164 

22.  I 
157 
I48 
73 
89 
185 
70 
130 
1.97 
0.68 
i.  06 

I.  10 

4 

I 

2.2 
7900 

3  600 
5  800 

248 

'45 
267 
109 
1  80 
98.3 
95-4 
96.9 

May  28 
12.  18  P.M 
June  3 
5.19  P.M. 
113-157 
14.12 
0.70 
2.09 
13.00 
0.52 
1.82 
1.40 
0.15 
0.27 
13454 
539 
I  906 
I3«>59 
464 
i  764 
I  257 
310 
587 
i  255 
44 
134 

0 

o 

0 
218 

8 
38 

20.8 
12.6 

16.2 

148 
89 

114 

9-5 
67 
57 
o 
6 
829 
400 
600 
10.70 
1.91 
4.41 

7.11 

5 

2 
4-o 
30600 
7900 
23  900 

June  3 

5.19  P.M. 

June  9 
g  45  A.M. 

158-183 
7-37 
0.80 
2.62 
7.08 
0.65 
2.40 

0-53 
0.15 

O.22 

8  224 

S23 
2555 

S  215 
750 
2448 

857 
380 

?22 
2*6 

45 

100 

o 
o 
o 

63 

6 
24 

20.  6 
13.0 
T7-3 
147 
92 

122 

12.4 

88 
37 
i 

10 

459 
1  60 
280 
7-48 
2.43 
4.06 

5-35 
3 

2 

2-3 
18  goo 
4300 
8  300 

June  g 
9.45  A.M. 
July  i 
g.oo  A.M. 
184-224 
8.90 
0.77 
3-32 
8.57 
0.57 
3.05 
0.45 
0.15 
0.27 

IO  II  I 

797 
3458 

10  175 

713 
3369 
794 
324 
577 
253 
53 
121 
O 
0 
O 
84 
7 
20 
21.0 
I6.7 
18.4 
149 
118 
131 
13-9 
98 

45 
i 
'3 
582 
200 
320 
8.58 
1.52 
4.84 

5-12 

3 

2 
2.1 
21  200 
6OOO 

10  400 

July  i 

g.OO  A.M. 

July  6 

g.I2  A.M. 
225-228 
3-73 
'•43 
2.  10 
3.12 
0.92 
I  .60 
0-55 
0.38 
0.50 
3513 
I  251 
1909 
3304 
935 
1635 
798 
735 
766 
296 
79 
234 

0 

o 
o 
81 
30 
32 
17.2 
16.8 
17.0 

122 
Jig 
120 

7-3 
5' 

12 
I 

4 
870 
870 
870 
5.58 
4-53 
4.91 

IO.2O 
3 
3 
3.0 

July  6 
9.12  A.M. 
July  22 
9.05A.M. 

229-248 

8.52 

1.48 

3-77 
8.27 
I  .22 
3-37 
0.60 
0.23 
0.40 
8553 
1578 
3688 
8359 
i  281 
345' 
936 
564 
744 
374 
53 
175 
o 
o 
o 
54 

IO 

25 

2O.  2 

15  4 
17.1 
143 
109 

121 
12.2 

86 
13 

2 

13 

560 
22O 
440 

7-55 
2.63 
4.62 

6.18 
2 
2 
2.O 
25400 

5  ooo 
8  loo 

130 
27 

July  22 
9.05  A.M. 
July  2g 
3-43  P.M. 
249-260 
4.40 
0.92 
2.43 
4.18 
0.73 
2.03 
1.30 
0.17 
0.40 
4  261 
647 
i  946 
3684 
617 
i  777 
83" 
484 
658 
742 
27 
'77 
O 
0 
0 

150 
17 

43 
15-6 
J3-3 
14.6 
in 
94 
103 
7.6 
53 
17 
o 
5 

2  170 
I  170 
I  530 
9.69 
3.20 
5-50 

10.00 

3 

2 

2-5 

33300 
9500 
22600 

3.16 

4-45 
3 
3 
3.0 
60  100 
41  600 
56  300 

Sio 

593 
i  153 
450 
773 
99-3 
98.0 
98.6 

3-23 

3.80 
4 

2 
3.0 
55400 
25  400 
4O6OO 

I  168 

419 
3276 
196 
726 
99.6 
92.4 
98.2 

3.46 

4.17 

5 

2 

3-2 
39600 
1  8  500 
26  ooo 

967 

614 
2  545 
76 
776 
99.6 
91.4 
97-o 

470 
27 
191 
99-9 
97-5 
99-2 

448 
'9 
72 
99-9 
96.4 
99.1 

I  OOO 
8 
76 
99-9 
94.6 
99-3 

357 
8 
58 
99-9 
97-5 
99-3 

646 

76 

314 

99-4 
98.1 
98.6 

240 


WATER  PURIFICATION  AT  LOUISVILLE. 
TABLE  No.  5. 

GRAND   TOTALS    AND   AVERAGES   FOR   THE    ENTIRE    INVESTIGATIONS. 


Warren 

Western 

Western 

System. 

System. 

System. 

Total   per  ods   in   days 

ion 

89.76 
83.76 
6.00 
347 
334 
2473  5iS 
2404357 
176285 
17  292 
49611 
6h.  27m. 
6h.  oim. 
26m. 
7405 
7  124 
528 
5i 
149 
19.9 
114 
2.70 
3.00 
96.7 

90.40 
86.68 
3.72 
272 
260 
3  f'6  1  073 
3077341 
162  997 
9739 
4387 
Sh.  aim. 
Sh.  oom. 
2im. 
II  808 
n  831 
627 
37 
18 
24.7 

100 

2.49 
2.65 
96.0 

25.81 
24-15 
1.66 
124 

122 
565  207 
526  112 
6077! 
17442 
22  422 

5h.  05m. 
4h    45m. 
2Om. 
4633 
4312 
498 
143 
ISS 
I5-I 
92 
2.90 
3-53 
97-4 

65.99 
62.72 
3-27 
261 
260 
i  773  994 
i  739628 
164658 
38371 

0 

6h.  osm. 
5h.  47«i- 
i8m. 
6823 
6  691 
633 
148 
o 
21.7 

154 
2.41 

2.72 

97.3 

~,  Service  . 

(  Wash  

Total  number  of  runs  i 

Total      quantities       of 
water    by    meter,    in 

.... 

f  Annlied 

|  Filtered  

<j  Wash  

Periods  of 
time  .... 

Average 

Per  run     Quantities 
of  water 

I 
Average  actual  rate  ... 

Average  grains  of  sul 
phate  of  alumina.  ... 
Average  bacterial  effic 

U    fill     ed 

(  Wash                     

1  Wash                                    

(  Million  gallons  per  acre  per  24  hours  . 
j  Per  gallon  of  applied  water  
~\  Per  gallon  of  net  filtered  water  

SUMMARY  AND   DISCUSSION   OF  DATA    OF   1895-96. 


o     < 
S3      5 


«=• 

II 

<a 


II 


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ji1! 

:.£•=      ,:  I^S      j  :| 

n  u 

A  i 

.   rt   it              .   rt  p         •     .   rt 

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c  ^ 

•  o  a«      :   •  o  —      ;   •  c  a. 

£  £     = 

—  (j  U  1 
4>  *-"*-•  ^ 
S  D  V  C 

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EC       c 

OJ     1>           < 

•  £  £     =  •  £  £     c   '  £ 

Z'-.:        Z  = 


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7)  !^ 


242 


WATER   PURIFICATION  AT  LOUISVILLE. 


OUTLINE   OF   THE   METHODS   FOLLOW KD   IN 

THE  DISCUSSION  OF  THE  RESULTS  OF 

THE  INVESTIGATIONS. 

At  the  outset  of  this  discussion  the  fact  is 
to  be  recorded  that  the  amount  of  strictly 
comparable  data  forms  only  a  small  propor 
tion  of  those  presented  in  the  foregoing 
tables.  This  was  due  to  conditions  which 
unavoidably  caused  results  to  be  influenced 
by  more  than  one  varying  factor  at  the  same 
time.  To  keep  conditions  parallel  with  re 
gard  to  certain  important  factors  was  imprac 
ticable,  owing  to  the  arrangements  under 
which  the  tests  were  conducted.  Neverthe 
less,  considerable  light  was  obtained  upon 
those  laws  which  appear  to  control,  practi 
cally  speaking,  the  efficiency  and  elements  of 
cost  of  purification  by  this  method.  This  is 
especially  true  of  the  laws  when  taken  as  a 
whole.  When  single  laws  or  principles  are 
considered,  it  will  be  found  that  in  many 
cases  they  are  intimately  associated  with 
others,  and  the  data  lead  to  valuable  and 
practical  suggestions,  rather  than  to  well-de 
fined  and  specific  conclusions.  This  was  not 
true  in  all  cases,  however,  as  much  definite 
information  of  practical  significance  was  ob 
tained. 

The  discussion  is  presented  under  five  main 
sections,  as  follows: 

1.  The    quality    of    the    Ohio    River    water 
after  purification,   with   reference   to   the   re 
spective  systems. 

2.  Prominent  factors,  which  influenced  the 
qualitative    efficiency    of    purification    in    the 
case  of  the  respective  systems. 

3.  Prominent  factors  which  influenced  the 
elements  of  cost  of  purification  in  the  case  of 
the  respective  systems. 

4.  Comparison  of  the  elements  of  cost  of 
purification,    by    the    respective    systems,    of 
twenty-five    million    gallons    of    Ohio    River 
water  daily,  based  on  the  foregoing  results. 

5.  General  conclusions. 

The  discussions  and  conclusions  in  this 
chapter  relate  solely  to  the  information  ob 
tained  up  to  August  i,  1896.  In  1897  addi 
tional  light  was  obtained  on  a  number  of 
important  points  connected  with  this  general 
method  of  purification,  as  is  stated  in  Chap 
ter  XV.  For  a  complete  understanding  of 


the  practical  significance  of  these  tests  it  is 
necessary  to  study,  together,  both  Chap 
ters  IX  and  XV,  but  it  must  be  borne  in  mind 
that  they  refer  to  distinctly  separate  data, 
which  were  obtained  under  different  condi 
tions. 

SECTION   No.    i. 

THE  QUALITY  OF  THE  Onio  RIVER  WATER 
AFTER  PURIFICATION,  WITH  REFERENCE 
TO  THE  EFFICIENCY  OF  THE  RESPECTIVE 

SYSTEMS. 

For  the  sake  of  explicitness  the  quality  of 
the  water  after  purification  is  discussed  with 
the  following  points  in  view: 

A,  Physical  character. 

B.  Chemical  character. 
C  .    Biological  character. 

It  will  be  remembered  that  this  method  was 
followed  in  Chapter  1.  where  the  composition 
of  the  Ohio  River  water  before  purification 
was  described;  and  reference  is  made  here  to 
that  chapter  for  detailed  data  for  comparison 
with  those  presented  in  this  chapter  and  the 
preceding  one. 


Appearance. — As  a  rule  the  appearance  of 
the  effluents  of  the  respective  systems  was 
satisfactory  with  regard  to  freedom  from 
turbidity.  Each  of  the  effluents  was  turbid 
at  times,  but  the  operation  of  the  systems  was 
usually  modified  promptly,  so  as  to  correct  a 
failure  in  appearance. 

In  the  case  of  the  Western  Systems,  but 
not  in  the  Warren  or  lewell  systems,  the 
effluents  were  usually  turbid  immediately 
after  washing  the  filters,  and  it  was  the  cus 
tom  to  waste  the  effluent  until  it  became  clear. 
Tn  the  Warren  and  Western  Pressure  systems, 
the  effluent  usually  became  turbid  after  the 
loss  of  head  had  reached  a  certain  but  varying 
amount,  and  in  these  systems  it  was  the  tur 
bidity  of  the  effluent  which  determined  the 
time  of  washing  the  filter.  This  was  true  in 
a  great  many  instances  of  the  Jewell  System, 
but  by  no  means  uniformly  so.  The  com 
position  of  the  river  water  with  its  minute 
particles  of  clay,  and  the  degree  of  coagula- 


SUMMARY   AND   DISCUSSION   OF  DATA    OF    1895-96. 


243 


tion  of  the  river  water  with  reference  to  the 
actual  conditions  of  nitration,  were  important 
factors  associated  with  the  appearance  of  the 
effluent,  as  will  be  evident  from  the  following 
portions  of  this  chapter. 

The  foregoing  summary  of  the  data  on  tlu 
appearance  of  the  several  effluents,  in  Table 
No.  i,  shows  that  the  effluent  of  the  Jewell 
System  was  the  most  satisfactory  in  this  re 
spect. 

Color. — As  the  river  water  itself,  inde 
pendent  of  its  suspended  matters,  is  practi 
cally  colorless  all  of  the  effluents  were 
naturally  satisfactory  with  regard  to  color. 
Whenever  they  showed  a  noticeable  color  it 
was  not  due  to  dissolved  coloring  matter  in 
the  filtered  water,  but  to  a  turbidity  which 
has  been  referred  to  under  "  Appearance." 

Taste. — The  taste  of  the  several  effluents 
was  satisfactory,  although  it  differed  some 
what  from  that  of  the  river  water,  owing  to 
the  varying  amounts  and  kinds  of  suspended 
matters  in  the  latter. 

Odor. — The  slight  musty,  aromatic  or 
vegetable  odor  of  the  river  water  was  sub 
stantially  unchanged  by  the  purification  of  the 
water  by  this  method.  In  practically  no  case 
was  the  odor  objectionable,  or  more  in 
tense  than  would  be  expected  from  a  surface 
water. 

Chemical  Character  of  the  Effluents. 

Organic  Matter. — \Yith  the  possible  excep 
tion  of  those  abnormal  conditions  when  the 
appearance  of  the  effluent  failed  to  be  satis 
factory,  the  organic  matter  in  the  river  water 
was  reduced  to  a  satisfactory  degree  by  each 
of  the  systems  of  purification.  The  summary 
of  the  data  upon  this  point,  presented  in  Table 
No.  2  of  this  chapter,  shows  the  percentages 
of  removal.  It  will  be  noted  that  practically 
all  of  the  suspended  organic  matter,  and  a  cer 
tain  amount  of  dissolved  organic  matter 
which  was  dependent  upon  the  quantity  of 
applied  sulphate  of  alumina,  were  removed 
from  the  water  in  the  case  of  each  of  the  re 
spective  systems  of  purification. 

Dissolved  Oxygen. — The  amount  of  free  at 
mospheric  oxygen  dissolved  in  the  water  was 
substantially  unchanged  by  treatment  bv  the 
Jewell  and  Western  Gravity  systems.  There 


was  a  slight  increase  as  a  rule  in  the  case  of 
the  Warren  System,  due  to  passage  of  the 
effluent  over  the  weir  by  which  the  rate  of 
filtration  was  regulated.  In  the  Western 
Pressure  System  there  was  apparently  no 
change  until  the  warm  weather  of  June  and 
July,  when  there  was  a  reduction  in  the 
amount  of  oxygen  dissolved  in  the  water. 
The  results  of  determinations  of  the  amounts 
of  oxygen  dissolved  in  the  river  water  and  in 
the  effluents  of  the  respective  systems  of  puri 
fication  are  given  in  the  following  table: 

PERCENTAGES  WHICH  THE  FREE  OXYGEN 
DISSOLVED  IN  THE  OHIO  RIVER  WATER, 
AND  IN  THE  EFFLUENTS  OF  THE  RESPEC 
TIVE  SYSTEMS  OF  PURIFICATION,  WAS  OF 
THAT  NECESSARY  FOR  SATURATION  AT 
THE  ACTUAL  TEMPERATURE. 


Temper- 

F.fflvj 

ems. 

Degrec. 

Water. 

Warren. 

Jewell. 

Western 
Grav.iy. 

Western 

1895 

Dec.    3 

7s 

Si 

78 

76 

So 

6 

So 

82 

78 

87 

86 

82 

1896 

86 

88 

84 

"     T7 

98 

Feb.  10 

5-9 

97 

"     26 
Mar.     4 

3-4 

100 

IOO 

92 

92 

99 

"      ii 

6-5 

9° 

88 

5.2 

98 

May    6 

23.1 

85 

96 

85 

83 

24.5 

"      2g 

24.7 

71 

87 

76 

85 

87 

80 

88 

So 

"      IS 

25.3 

78 

87 

78 

68 

26.S 

So 

85 

67 

July    9 
"     18 

25-5 
25-6 

72 
71 

78 
83 

76 
77 

""76 

60 

Undecomposed  Sulphate  of  Alumina. — The 
question  of  the  passage  of  undecomposed  sul 
phate  of  alumina  was  presented  and  discussed 
with  care  in  Chapter  III.  It  may  be  again 
stated  that  with  the  skill  and  care  requisite 
for  the  efficient  and  economical  operation  of 
a  system  of  purification  by  this  method  there 
is  no  occasion  for  the  passage  into  the  efflu 
ent  of  undecomposed  chemical,  applied  for 
the  purpose  of  coagulation,  so  far  as  can  be 
judged  from  the  quality  of  the  Ohio  River 
water  met  with  during  these  investigations. 
The  only  instance  where  the  effluent  was  acid, 
due  to  an  excess  of  sulphate  of  alumina,  for 


244 


WATER   PURIFICATION  AT  LOUISVILLE. 


several  days  in  succession  was  in  the  case  of 
the  Jewell  System  during  July. 

This  was  due  solely  to  carelessness  on  the 
part  of  the  operators  of  the  system.  In  all  of 
the  systems  the  lack  of  adequate  provisions 
for  subsidence  made  the  possibilities  of  this 
occurrence  much  greater  than  should  be  per 
mitted  in  practice. 

Carbon  Dioxide. — From  a  practical  point  of 
view  the  amount  of  carbon  dioxide,  more 
familiarly  known  as  carbonic  acid  gas  and  dis 
solved  in  water  in  the  form  of  free  carbonic 
acid,  is  of  considerable  significance  by  virtue 
of  the  part  which  it  plays  in  the  corrosion  of 
"iron  pipe,  tanks  and  boilers.  Corrosion  of 
uncoated  iron  receptacles  for  water  by  the 
joint  action  of  carbonic  acid  and  free  at 
mospheric  oxygen  gas  dissolved  in  the  water 
is  substantially  as  follows: 

Carbonic  acid  attacks  the  iron,  when  in 
completely  protected  by  paint  or  other  prep 
arations,  and  forms  what  appears  to  be  the 
ferrous  carbonate  of  iron. 

The  oxygen  in  the  water  changes  this  com 
pound,  formed  by  the  action  of  the  carbonic 
acid,  into  the  insoluble  ferric  hydrate  of  iron, 
and  at  the  same  time  liberates  carbonic  acid 
gas.  This  carbonic  acid  attacks  more  iron 
and  the  action  goes  on  by  a  repetition  of  this 
process,  aided  by  such  additional  amounts  of 
carbonic  acid  and  oxygen  as  the  water  brings 
to  the  attacked  surface.  The  rate  at  which 
the  iron  surface  is  corroded  depends  upon  a 
series  of  factors,  the  relative  importance  of 
which  is  not  accurately  known.  There  is  no 
conclusive  proof,  however,  so  far  as  is  known, 
that  the-action  is  a  self-limited  one  in  the  case 
of  pipes  and  tanks.  In  boilers  the  high  tem 
perature  drives  off  these  gases,  and  corrosion 
.appears  to  be  more  irregular  and  less  marked, 
and  would  be  located  at  the  water  line. 

By  means  of  this  process  there  is  formed 
in  the  iron' a  depression  of  greater  or  less  size, 
according  to  the  period  of  exposure  and  other 
conditions.  In  this  depression,  and  reaching 
out  from  it,  is  a  formation  which  is  called  a 
tubercle.  These  tubercles  have  been  found  to 
consist  principally  of  iron  hydrate  or  oxide, 
together  with  a  little  silica,  lime,  magnesia 
and  carbonic  acid,  and  such  compounds  from 
the  water  as  are  coagulated  by  the  iron  hy 
drate.  It  will  be  noted  that  this  action  is  an 


illustration  of  the  principles  employed  in  the 
preliminary  treatment  of  water  by  the  Ander 
son  process  of  purification,  with  which  you 
are  familiar  in  a  general  way. 

This  corroding  action  is  possessed  by  the 
Ohio  River  water  before  purification,  by 
virtue  of  the  carbonic  acid  and  oxygen  dis 
solved  in  it.  Whether  or  not  the  other  sub 
stances  in  the  river  water  influence  to  an  ap 
preciable  degree  (practically  speaking)  the 
corrosion  of  iron  is  not  now  accurately 
known.  But  concerning  such  ingredients,  if 
any  are  present  they  are  in  solution  and  there 
are  strong  reasons  for  the  belief  that  they 
would  be  substantially  unaffected  by  the  treat 
ment  in  question.  The  corrosion  of  iron  by 
the  river  water  was  shown  by  an  inspection 
of  the  water-pipes  at  the  laboratory  and 
pumping  station.  In  the  Ohio  River  water 
after  purification  by  this  method,  this  corrod 
ing  action  is  apparently  increased,  practically 
speaking,  by  an  amount  proportional  to  the 
composition  and  quantity  of  alum  or  sulphate 
of  alumina  added  to  the  water  to  effect 
coagulation.  This  increased  corroding  action 
is  indicated  by  the  following  experiment: 

On  July  8,  1896,  two  glass  flasks  contain 
ing  a  considerable  quantity  of  cast-iron  bor 
ings  were  filled  with  river  water  and  Jewell 
effluent,  respectively.  The  amount  of  oxy 
gen  dissolved  in  the  water  of  the  two  flasks 
was  practically  the  same — about  75  per  cent, 
of  that  necessary  for  saturation.  The  effluent 
of  course  contained  more  carbonic  acid,  due 
to  the  decomposition  of  the  applied  sulphate 
of  alumina,  which  on  that  day  averaged  4.67 
grains  per  gallon.  The  flasks  and  their  con 
tents  were  allowed  to  stand  forty-eight  hours 
with  occasional  stirring.  Analyses  were  then 
made  with  the  following  results: 
PARTS  PER  MILLION. 


Sample. 

Carbonic  Acid 
Before 

Dissolved  Iron 
After 

River  water 

8.70 

Jewell  effluent  

40.9 

21.30 

The  above  experiment  was  repeated  with 
like  results,  and  serves  to  show  the  increased 
corroding  action  of  the  water  after  purifica 
tion.  These  results,  however,  must  not  be 
taken  as  a  basis  for  computation  of  the  rate  of 
corrosion  in  actual  practice,  because  the  vari- 


SUMMARY  AND   DISCUSSION  OF  DATA    OF   1895-96. 


ous  conditions  affecting  this  action  were  not 
sufficiently  parallel  to  yield  data  for  any  other 
purpose  than  that  for  which  the  experiment 
was  made. 

To  what  extent  steam  boilers,  and  cast  iron, 
wrought  iron  or  other  metal  used  for  dis 
tributing  and  service  pipes  or  fittings,  in  the 
case  of  this  water,  are,  or  may  be,  effectually 
protected  from  corrosion  by  a  suitable  sur 
face  coating,  is  a  matter  which  the  writer  has 
not  investigated,  and  upon  which  he  has  no 
opinion  to  express  at  this  time. 

In  Chapter  I  it  was  shown  that  during 
June  and  July,  1896,  the  Ohio  River  water 
contained  from  21.1  to  30.8  parts  per  million 
of  carbonic  acid  gas  by  weight.  At  some 
seasons  of  the  year  the  water  doubtless  con 
tains  much  more  than  the  above  quantity  of 
carbonic  acid.  The  evidence  indicates  that  in 
Nov.,  1895,  it  was  at  least  75  parts.  A  con 
siderable  portion  of  the  carbonic  acid,  and  at 
times  perhaps  all  of  it,  is  engaged  in  holding 
the  carbonates  of  calcium  and  magnesium  in 
solution  in  the  form  of  bicarbonates.  The 
bicarbonates  are  not.  stable  compounds,  rel 
atively  speaking,  and  there  is  substantial 
proof  that  they  give  up  their  carbonic  acid  to 
facilitate  the  corroding  action  in  question. 
With  regard  to  the  relative  rates  of  corroding 
action  by  free  carbonic  acid  gas  and  partially 
engaged  carbonic  acid  in  the  form  of  bicar 
bonates,  there  are  no  available  data  to  lead 
to  a  satisfactory  expression  of  opinion. 

The  amount  of  carbonic  acid  gas  liberated 
by  the  decomposition  of  alum  or  sulphate  of 
alumina,  is  capable  of  both  approximate  deter 
mination  and  estimation.  The  latter  requires, 
however,  an  exact  knowledge  of  the  amount 
and  composition  of  the  applied  alum  or  sul 
phate  of  alumina.  From  the  data  presented 
in  Chapters  I  and  II  the  amount  of  carbonic 
acid  liberated  in  the  water  by  the  decomposi 
tion  of  the  applied  chemical  during  these 
tests  may  be  estimated  with  sufficient  close 
ness  for  practical  purposes. 

The  amount  of  liberated  carbonic  acid  gas 
per  unit  quantity  of  applied  chemical  varied 
somewhat  in  the  several  lots  which  were  used, 
owing-  to  the  different  percentages  of  sul 
phuric  acid.  But  taking  a  chemical  of  average 
composition,  and  assuming  that  the  chemical 
united  wholly  with  the  alkaline  compounds, 


and  not  with  organic  or  suspended  matters, 
the  amount  of  liberated  carbonic  acid  gas 
may  be  adequately  shown  as  follows: 

In  the  case  of  the  potash  alum  used  by  the 
Western  Company  each  grain  per  gallon 
would  liberate  about  2.5  parts  per  million  of 
carbonic  acid  gas  by  weight. 

With  the  several  different  lots  of  sulphate 
of  alumina,  the  parts  per  million  by  weight  of 
liberated  carbonic  acid  gas  would  range  from 
3.6  to  4.0,  and  average  about  3.7,  for  each 
grain  per  gallon  of  applied  chemicals.  These 
figures  refer  solely  to  the  liberation  of  chemi 
cally  combined  carbonic  acid  gas.  In  addi 
tion  thereto,  in  the  case  of  bicarbonates  an 
equal  amount  of  carbonic  acid,  partly  en 
gaged  by  holding  calcium  carbonate  in  solu 
tion,  would  also  be  set  free-.  It  is  very  ques 
tionable,  however,  whether  this  last  action 
would  affect  corrosion  appreciably,  if  at  all. 

From  the  above  statements,  together  with 
the  foregoing  tabulations  in  detail  of  the 
amounts  of  chemical  applied  by  the  respec 
tive  systems,  correct  information  may  be  ob 
tained  as  to  the  average  quantity  of  carbonic 
acid  gas  liberated  in  each  case,  for  runs,  days 
or  periods. 

Some  observations  worthy  of  mention 
were  made  upon  the  wrought-iron  reservoir 
used  for  the  storage  of  filtered  water  for  use 
in  washing  the  filters.  Throughout  the  in 
vestigations,  this  iron  reservoir,  which  was 
not  protected  on  its  inner  surface  by  a  coating 
of  paint,  tar  or  other  material,  was  practically 
filled  with  filtered  water.  In  fact  its  use  for 
this  purpose  began  early  in  July,  1895.  From 
the  close  of  the  tests  on  Aug.  r,  1896,  the 
reservoir  remained  full  of  filtered  water,  in  an 
undisturbed  condition,  until  Oct.  17,  when 
one  of  the  systems  was  operated  for  a  few 
hours.  It  then  remained  undisturbed  for 
another  month,  when  it  was  drained.  Several 
days  after  draining,  the  inner  surface  of  the 
iron  was  examined  and  found  to  be  corroded 
to  a  considerable  degree.  Tubercles  were 
found  ranging  in  size  from  that  of  "a  pin-head 
to  about  0.4  inch  in  height,  and  i  inch  in  di 
ameter  as  a  maximum.  Their  size  was  very 
variable.  It  is  of  course  certain  that  the  cor 
roding  action  was  increased  somewhat  by 
the  acid  effluent  of  the  Jewell  System  during 
a  number  of  successive  days  in  July.  This 


246 


WATER  PURIFICATION  AT  LOUISVILLE. 


inexcusable  acidity  was  perhaps  not  the  chief 
factor,  however,  as  the  effluents  regularly  had 
considerable  corroding  action,  as  was  shown 
by  the  iron  in  the  effluents  which  stood  over 
Sunday  in  the  iron  outlet  pipes. 

A  more  exhaustive  study  of  this  subject 
was  made  in  1897,  ail('  m  passing  it  may  be 
noted,  the  corroding  action  of  the  undecom- 
posed  chemical  in  the  effluent  even  at  rare 
intervals  was  of  great  significance,  as  it  ac 
celerated  the  action  of  the  carbonic  acid.  The 
suspended  matter  in  the  river  water  forms  a 
partial  protective  coating  to  the  metal,  and 
this  explains  for  the  most  part  the  results  of 
the  experiment  on  July  8,  1896.  Further 
more,  the  more  extended  data  of  1897  showed 
that  the  evidence  obtained  in  1896  indicated 
an  abnormally  high  percentage  increase  of 
carbonic  acid  after  purification.  Additional 
information  upon  this  subject  is  given  in 
Chapter  XV. 

Analysis  of  one  of  the  tubercles  mentioned 
above  showed  it  to  be  composed  very  largely 
of  iron  in  the  ferric  oxide  state,  with  a  small 
amount  of  calcium  carbonate  (lime). 

The  percentage  composition  was  found  to 
be  as  follows: 

Water   1 1.42 

Silica  (SiO2) 0.19 

Oxide  of  iron  (Fe2O3),  by  difference. .  .    85.1 1 

Alumina  (A12O3) Trace 

Lime  (CaO) 1.77 

Magnesia  (MgO) 0.03 

Sulphuric  acid  (SO:i) 0.08 

Carbonic  acid  (CO2),  by  estimation.  .  .  1.40 
Organic  matter Trace 

In  concluding  this  account  of  the  increased 
corroding  action  of  the  water  after  purifica 
tion,  due  to  increased  amounts  of  carbonic 
acid  gas  proportional  to  the  quantity  of  alum 
or  sulphate  of  alumina  added  to  the  water,  it 
may  be  stated  that  the  adoption  of  this 
method  of  purification  would  call  for  especial 
care  in  coating  the  inner  surface  of  pipes,  and 
for  all  feasible  means  of  keeping  the  amount 
of  applied  sulphate  of  alumina  at  a  minimum. 

So  far  as  experience  teaches  us.  the  corrod 
ing  action  of  this  water  before  and  after  puri 
fication,  on  lead,  would  not  give  trouble,  be 
cause  it  quickly  forms  a  coating  by  itself 
which  protects  the  lead  from  further  action. 


It  may  also  be  added,  that  the  carbonic 
acid  gas  may  be  removed  from  water  by  lime 
water  or  caustic  soda,  with  subsequent  sub 
sidence  or  filtration.  It  is  not  probable,  how 
ever,  that  such  steps  would  ever  be  necessary. 

Passage  of  Lime  from  the  Form  of  Carbon 
ates  to  that  of  Sulphate. — It  has  been  explained 
in  Chapter  111  that  the  alkalinity  of  this  water 
was  produced,  for  the  most  part,  if  not 
wholly,  by  the  carbonates  and  bicarbonates 
of  lime  and  magnesia,  respectively,  and 
that  it  was  reduced  by  an  amount  approxi 
mately  proportional  to  the  quantity  of  alum 
or  sulphate  of  alumina  added  to  it.  With 
sulphate  of  alumina  of  average  composition 
the  alkalinity  has  been  found  by  actual  tests  to 
be  reduced  about  8.1  parts  per  million  for 
i  grain  of  this  chemical  added  to  i  gallon  of 
ordinary  river  water.  This  means  practi 
cally,  since  the  evidence  indicates  that  the  lime 
is  more  abundant  than  magnesia,  that  this 
amount  of  lime  and  magnesia,  but  principally 
lime,  is  converted  from  the  form  of  carbonate 
or  bicarbonate  to  that  of  sulphate.  That  is 
to  say,  the  permanent  hardness  or  incrusting 
constituents  is  increased  by  about  8.1  parts 
per  million,  according  to  the  conventional 
method  of  expressing  permanent  hardness  in 
terms  of  calcium  carbonate.  The  actual 
weight  of  the  compounds  increasing  the  in- 
crusting  constituents  would  be  more  than 
this,  because  calcium  sulphate  weighs  1.37 
times  as  much  as  an  equivalent  amount  of 
calcium  carbonate. 

With  potash  alum,  such  as  was  used  by  the 
Western  Company,  the  application  of  i  grain 
per  gallon  was  found  to  reduce  the  alkalinity, 
and  increase  the  incrusting  constituents 
about  4.5  parts  per  million. 

The  data  presented  in  Chapter  I  show  that 
the  incrusting  constituents  of  the  Ohio  River 
water  ranged  from  30  to  51  parts  per  million. 
when  tested  during  this  period.  With  the 
above  data  on  the  increase  of  incrusting  con 
stituents  due  to  the  application  of  alum  or  sul 
phate  of  alumina,  and  the  foregoing  records 
of  the  amounts  of  these  chemicals  employed 
by  the  respective  systems,  a  correct  idea  may 
be  obtained  as  to  the  increased  incrusting 
constituents  of  the  several  effluents. 

It  is  the  amount  of  incrusting  constituents 
of  a  water,  due  to  the  chlorides,  nitrates  and 


SUMMARY  AND   DISCUSSION  OF  DATA    OF   1895-96. 


247 


sulphates  of  lime  and  magnesia,  which  chiefly 
determines  its  fitness  for  boiler  use.  When 
proper  care  is  taken  of  boilers,  it  appears  that 
the  Ohio  River  water  does  not  give  serious 
trouble  except  during  low  water  in  the  fall, 
by  the  formation  of  boiler  scale;  although  the 
suspended  matter  in  the  water  forms  a  sludge, 
which  requires  frequent  flushing  of  the  boil 
ers,  and  occasional  removal  by  manual  labor. 
With  the  probable  exception  of  magnesium 
chloride,  due  to  its  tendency  to  decomposi 
tion  and  formation  of  hydrochloric  acid,  there 
is  no  more  objectionable  ingredient  of  water 
for  boilers  than  sulphate  of  lime.  This  com 
pound,  which  is  formed  by  the  addition  of 
alum  or  sulphate  alumina  to  water,  as  ex 
plained  above,  and  which  is  soluble  at  ordi 
nary  temperature,  produces  at  boiler  tempera 
tures  a  fine  hard  scale,  in  which  practically 
all  of  the  suspended  matters  of  the  water  be 
come  embodied,  when  those  matters  consist 
of  fine  clay.  In  the  case  of  heavy  mud,  these 
incrustations  are  attached  to  the  sludge. 
Unless  removed,  the  scale  formed  in  this  man 
ner  eventually  causes  a  marked  waste  in  the 
consumption  of  fuel  by  retarding  the  trans 
mission  of  heat  to  the  water;  and  it  is  com 
pletely  removed  with  great  difficulty. 

Such  a  scale  was  found  in  Boiler  No.  3  at 
the  pumping  station  of  this  Company,  as  you 
have  been  advised. 

This  boiler  was  said  to  have  been  filled  with 
the  effluent  of  the  Warren  and  Jewell  systems 
on  July  7.  During  the  next  run  of  five  weeks, 
muddy  river  water  was  introduced  to  replace 
the  steam  which  was  not  condensed  and  re 
turned  from  the  engine  to  the  boiler.  The 
boiler  was  carefully  examined  after  one  sub 
sequent  run  to  this  one  was  made,  without 
cleaning  during  the  interval  of  rest.  On  ex 
amination  the  tubes  and  plates  were  found  to 
be  covered  with  a  hard  rough  incrustation 
such  as  above  described.  This  was  especially 
noticeable  on  the  iron  plates  around  the  fire 
box.  In  places  there  were  evidences  of  cor 
rosion.  A  portion  of  this  incrustation  was 
removed  and  analyzed,  with  results  which 
show  the  following  percentage  composition: 

Water,  with  organic  and  volatile  mat 
ters  ifi-52 

Silica  (SiO2) 19.65 


Oxide  of  iron  (Fe2O3) 4.30 

Alumina  (A12O3) 9.66 

Lime  (CaO) 37-97 

Magnesia  (MgO) 0.60 

Soda  (Na2O) Undetermined 

Potash  (K2O) Undetermined 

Chlorine  (Cl) Trace 

Nitric  acid  (N2O5) Trace 

Carbonic  acid  (CO2) Trace 

Sulphuric  acid  (SO3) 1 1.87 

The  alumina  which  was  found  in  the  in 
crustation  came  from  the  silicates  (clay)  of 
the  river  water  subsequently  added  to  the 
boiler,  and  not  from  the  chemical  applied 
in  the  course  of  purification. 

At  the  time  when  the  boiler  was  said  to 
have  been  filled  with  the  effluent,  there  were 
about  four  grains  per  gallon  of  sulphate  of 
alumina  being  added  to  the  river  water  on  an 
average.  This  practically  doubled  the  in- 
crusting  constituents  of  the  water,  and  added 
to  the  effluent  about  44  parts  per  million  of 
calcium  sulphate  by  weight.  This  sulphate 
was  soluble  as  it  entered  the  boiler,  but  the 
high  temperature  caused  it  to  be  insoluble, 
with  the  result  that  a  very  hard  scale  was 
formed,  which  included  a  large  portion  of  the 
suspended  matter  of  the  water  subsequently 
added  to  the  boiler. 

In  fact  the  analyses  show  that  less  than  20 
per  cent,  of  the  incrustation  was  composed  of 
sulphate  of  lime. 

The  above  experience  shows  that  all  rea 
sonable  steps  should  be  taken  to  keep  the 
amount  of  applied  sulphate  of  alumina  to  a 
minimum.  In  this  connection,  however,  it  is 
to  be  stated  that  the  amount  of  sulphate  of 
alumina  added  to  the  river  water  on  the  date 
when  the  boiler  was  said  to  have  been  filled, 
was  about  50  per  cent,  greater  than  the  aver 
age  amount  employed  during  these  tests. 

Furthermore,  the  mud,  silt  and  clay  in  the 
water  subsequently  put  into  the  boiler,  added 
very  materially  to  the  incrustation,  as  shown 
by  the  results  of  the  chemical  analyses. 

By  the  use  of  soda,  it  is  possible  to  remove 
the  sulphates  of  lime  and  magnesia  from  the 
water;  and  trisodium  phosphate  will  also 
serve  this  purpose,  should  manufacturing  -es 
tablishments  choose  to  remove  these  ingredi 
ents  before  the  water  enters  the  boilers. 


WATER  PURIFICATION  AT  LOUISVILLE. 


Further  discussions  of  the  incrusting  power 
of  the  Ohio  River  water,  before  and  after  puri 
fication,  with  additional  data,  will  be  found  in 
Chapter  XV.  At  this  point,  it  may  be  briefly 
noted  that  when  the  river  water  is  muddy 
and  requires  the  largest  quantities  of  coagu 
lant,  the  incrusting  constituents  naturally 
present  in  the  water  are  so  low  in  amount 
that  the  total  incrusting  power  of  the  efflu 
ent  would  be  much  less  than  that  of  the 
natural  river  water  during  the  fall  months. 

Biological  Character  of  the  Effluents. 

Microscopical  Organisms. — The  tables  in 
Chapter  VIII  show  that  practically  no 
diatoms,  algae  or  other  microorganisms, 
which  may  be  readily  recognized  by  the  aid 
of  the  microscope,  were  present  in  the  efflu 
ents.  This  would  be  naturally  expected  un 
der  the  circumstances,  owing  to  their  greater 
size  when  compared  with  the  bacteria.  It  is 
to  be  noted,  however,  that  very  few  organ 
isms  of  this  nature  were  found  in  the  river 
water,  owing  to  unfavorable  natural  condi 
tions  existing  there. 

In  this  connection  there  arises  a  question 
of  much  practical  significance,  as  was  pointed 
out  in  a  communication  addressed  to  you 
on  July  IT,  1896;  that  is,  the  conditions  un 
der  which  the  growth  of  microorganisms, 
notably  alga?,  in  the  effluents  could  be  pre 
vented  during  the  period  when  the  water  is 
stored  prior  to  distribution.  In  the  case  of  all 
the  effluents  the  conditions  for  growth  of 
algae  would  be  favorable  in  the  presence  of 
sunlight;  and  should  these  forms  once  be 
come  established  in  the  distributing  reservoir 
the  probability  of  the  production  of  objec 
tionable  tastes  and  odors  in  the  effluent,  no 
matter  how  satisfactory  was  its  character  as 
it  left  the  filters,  would  be  a  very  serious  state 
of  affairs. 

There  are  no  specific  data  to  offer  upon  this 
subject. 

Bacteria. — The  removal  of  bacteria  from  a 
water  which  at  times  shows  such  marked 
proof  of  sewage  pollution  as  is  the  case 
with  the  Ohio  River,  is  a  very  important 
matter.  This  is  particularly  so  in  view  of  the 
rapidly  increasing  population  in  the  Ohio 
River  valley,  and  the  set  of  data  upon  this 


System. 

Bacterial  Kfficie 

icy. 

Jewell  -  

Western  Pressure  

97-3 

point  was  made  as  complete  as  practicable. 
Comprehensive  summaries  of  these  data  have 
already  been  presented  in  this  chapter.  The 
bacterial  efficiency  of  the  respective  systems, 
as  shown  by  the  total  averages,  was  as  fol 
lows: 


The  above  results  are  not  directly  compara 
ble,  because  the  length  of  service  and  the 
condition  of  the  river  water  during  service 
were  quite  unlike,  as  shown  by  the  data  of 
each  of  the  twenty  periods  of  different  grades 
of  river  water. 

Excluding  the  Western  Gravity  System  on 
the  grounds  of  failure  to  purify  enough  water, 
when  the  river  water  was  in  a  muddy  condi 
tion,  to  wash  its  own  sand  layer,  and  taking 
the  averages  of  all  those  periods  in  which  the 
remaining  systems  were  in  operation  without 
any  prescriptions  from  this  Company,  the  fol 
lowing  bacterial  efficiencies  are  obtained: 


Syste 


Warren 

Jewell 

Western  Pressure. 


98.5 
97-9 
97-4 


The  above  figures  show  the  relative  effi 
ciency  which  the  systems  possessed  in  the  re 
moval  of  bacteria  from  the  river  water.  Dur 
ing  the  early  part  of  the  tests  the  bacterial 
efficiency  was  irregular  and  unsatisfactory  at 
times  in  the  case  of  all  the  systems,  but  least 
so  in  the  case  of  the  Warren.  This  was  due 
in  part  to  limitations  of  the  devices  em 
ployed  in  the  respective  systems,  and  in 
part  to  a  lack  of  care  and  skill  in  adapting 
the  operation  of  the  system  to  meet  the  re 
quirements  of  the  rapidly  varying  character 
of  the  river  water.  In  February  and  March 
the  bacterial  efficiencies  of  the  systems,  speak 
ing  in  general  terms,  were  so  unsatisfactory 
that  an  official  communication  was  addressed 
on  March  16  to  the  operators  of  the  systems. 
The  request  was  made  among  others  that  they 
should  keep  the  bacterial  efficiency  of  their 
systems  above  97  at  all  times  when  the  num 
ber  of  bacteria  per  cubic  centimeter  in  the 


SUMMARY  AND  DISCUSSION  OF  DATA    OF   1895-96. 


249 


river  water  exceeded  7000,  and  when  the 
bacteria  in  the  river  water  were  less  than  this 
number  there  should  not  be  more  than  200 
per  cubic  centimeter  in  the  effluents. 

Following  this  official  request  for  greater 
uniformity  in  bacterial  efficiency,  the  applica 
tion  of  chemicals  and  the  rate  of  filtration,  a 
number  of  changes  and  improvements  were 
made  in  the  systems. 

As  a  rule  the  removal  of  bacteria  from  that 
time  to  the  close  of  the  test  was  satisfactory, 
provided  we  disregard  the  amount  of  chemi 
cals  employed  to  effect  the  purification. 

There  was  one  prominent  point  of  much 
practical  value  learned  in  connection  witli  the 
bacterial  efficiency  of  the  systems.  The 
opinion  has  generally  prevailed  that  the  qual 
ity  of  the  effluent  of  a  filter  of  the  type  em 
ployed  in  these  tests  would  not  be  satisfactory 
immediately  after  washing  the  sand  layer,  and 
for  some  minutes  it  would  be  necessary  to 
waste  the  filtered  water.  The  satisfactory 
bacterial  results  obtained  from  the  Warren 
and  Jewell  systems,  in  which  the  sand  layer 
was  quite  thoroughly  washed  as  a  rule,  show 
clearly  that  the  unsatisfactory  quality  of  the 
filtered  water  just  after  washing  is  not  an  in 
herent  feature  of  this  type  of  filters  under  the 
existing  conditions,  but  a  consequential  one, 
arising  from  incomplete  washing  of  the  sand 
layer,  and  other  factors. 

Inspection  of  the  results  showing  the  aver 
age  bacterial  efficiency  of  the  systems  indi 
cates  them  to  be  fairly  satisfactory  when  com 
pared  with  available  data  upon  the  efficiency 
of  filters  of  the  English  type.  Such  compari 
sons  of  data,  however,  require  the  careful  con 
sideration  of  several  facts.  In  the  first  place, 
the  growths  of  harmless  bacteria  generally 
recognized  to  prevail  to  a  greater  or  less  de 
gree  in  the  underdrains  and  lower  portions 
of  filters  of  the  English  type,  did  not  become 
established  to  any  marked  degree  in  the  cor 
responding  portions  of  these  filters  of  the 
American  type,  owing  evidently  to  the  wash 
ing  of  the  sand  layer  at  frequent  intervals. 
This  was  especially  true  of  the  filters  of  the 
Warren  and  Jewell  systems,  in  which  the  thor 
oughness  of  washing  was  enhanced  by  the 
accompanying  agitation  of  the  sand.  Another 
fact  bearing  directly  upon  this  point  is,  that 
if  any  slight  growth  of  bacteria  within  the 


lower  portions  of  a  filter  of  the  American 
type  should  take  place,  the  rate  of  filtration 
would  cause  the  bacteria  to  be  diluted  in  the 
effluent  to  about  fifty  times  the  extent  that 
would  be  the  case  in  English  tillers.  These 
facts,  together  with  the  results  of  numerous 
comparative  observations  of  the  species  of 
bacteria  in  the  water  before  and  after  purifi 
cation,  show  that,  in  order  to  insure  to  the 
consumers  of  the  same  water  the  same  protec 
tion  from  disease  germs,  the  bacterial  effi 
ciency  by  this  method  of  purification  must  be 
somewhat  higher  than  in  the  case  of  English 
filters. 

Several  years  ago  it  was  demonstrated  by 
a  series  of  separate  investigations  in  different 
parts  of  the  world,  that  English  filters  were 
not  "  germ-proof,"  but  with  skill  and  care  in 
their  construction  and  operation,  they  could 
be  made  very  nearly  so.  It  follows  from  the 
experience  gained  in  these  tests,  as  stated 
above,  that  skill  and  care  are  apparently  more 
necessary  in  the  case  of  the  method  of  puri 
fication  as  practiced  and  investigated  in  these 
tests,  than  in  the  case  of  the  English  filters. 
With  more  adequate  provision  for  subsidence, 
the  necessary  skill  and  attention  in  operation 
would  be  materially  reduced.  This  fact  of  not 
being  "  germ-proof  "  was  confirmed  by  the 
marked  similarity  from  time  to  time  of  the 
bacteria  in  the  water  before  and  after  purifi 
cation.  Evidence  upon  this  point  was  also 
obtained  from  the  artificial  application  of  bac 
teria,  which  in  their  life-history  in  water  re 
semble  the  bacillus  generally  recognized  as 
the  specific  germ  of  typhoid  fever. 

Bacillus  Prodigiosiis. — This  germ  was  ap 
plied  to  the  filters  of  each  of  the  systems  on  a 
number  of  different  occasions  during  the 
month  of  July,  1896.  It  was  not  considered 
prudent  to  apply  these  germs  to  the  filters 
at  an  earlier  period.  The  reason  of  this  was 
to  guard  against  the  possibility  of  having  any 
bacterial  growth  within  the  filter,  if  such 
should  occur,  attributed  to  any  actions  of  the 
Water  Company.  In  passing,  it  may  be 
added  that  the  introduction  of  Bacillus 
prodigiosns  requires  the  addition  to  the 
water  of  a  certain,  but  very  small,  amount  of 
organic  matter  in  which  the  germs  were 
grown.  When  these  germs  were  applied  to 
•  the  filters  it  was  done  very  cautiously,  and 


25° 


WATER   PURIFICATION  AT  LOUISVILLE. 


with  scarcely  an  appreciable  addition  to  the 
amount  of  organic  matter  naturally  present  in 
the  water.  The  method  consisted  of  applying 
to  the  water  above  the  sand  layer  a  measured 
quantity  of  a  solution  which  contained  mil 
lions  of  this  germ  to  each  cubic  centimeter. 
These  applications  were  made  every  five  min 
utes  for  several  hours,  and  the  applied  germs 
distributed  in  the  water  as  uniformly  as  prac 
ticable.  During  these  applications,  samples 
of  the  effluent  were  collected  at  frequent  in 
tervals  for  analysis. 

The  results  of  these  applications  of  Bacillus 
prodigiosns  to  the  several  filters  are  summa 
rized  in  the  next  table.  They  show  clearly 
that  under  the  existing  conditions  an  appre 
ciable  number  of  these  germs  was  able  to 
pass  through  the  filters.  Owing  to  the  lim 
ited  amount  of  data,  all  of  which  were  ob 
tained  under  a  narrow  range  of  conditions, 
they  are  of  little  value  in  the  consideration 
of  the  absence  of- bacterial  growths  within  the 
filters. 

SUMMARY   OF    THE    RESULTS    OF   THE    APPLI 
CATION      OF      BACILLUS      PRODIGIOSUS     TO 


Number  of 

Applied 

Number 

Number  of  B.  pro 

JiRiosus 

B  prodigi- 

of 

Average 

rubicren- 

HReof 

Effluent 

Rvmoval 

Filtered    'Analyzed       Max.           Min. 

Average. 

WARREN  FILTER. 

July    9 
"     16 

465 
3470 

20 
IS 

IS 
1  6 

o 
o 

3 

7 

99.4 
99.8 

"     24         800 

720 

0.7 

99.9 

"     28         150 

28     :         4           o 

0.2            99.9 

JEWELL  FILTER. 

July    3 

170           23              3 

o 

0.4 

99.8 

"     18 

I  170           35 

4 

o 

I                 99.9 

"     29 

350           29 

3 

0 

I 

99-7 

WESTERN  GRAVITY  FILTER. 

July  II          975 

21 

6 

o 

2 

99.8 

"     24         940           23 

29 

o 

10               98.9 

WESTERN  PRESSURE  FILTER. 

July  14 

450 

33 

19 

o 

3 

99-3 

"      21 

480 

22 

27 

o 

7 

98.6 

SECTION  No.  2. 

PROMINENT  FACTORS  WHICH  INFLUENCED 
THE  QUALITY  OF  THE  OHIO  RIVER 
WATER  AFTER  PURIFICATION  IN  THE 
CASE  OF  THE  RESPECTIVE  SYSTEMS. 

The  following  pages  contain  a  brief  discus 
sion  of  the  influence  of  the  factors  which  from 


a  practical  point  of  view  appeared  to  be  of  the 
most  importance  in  the  purification  of  this 
water.  As  a  rule  these  factors  affected  both 
the  quality  of  the  effluents  and  the  cost  of 
treatment.  Their  influence  upon  the  quality 
of  the  effluents  is  considered  in  this  section, 
and  their  relation  to  the  cost  of  treatment 
is  presented  in  the  next  section  of  this  chap 
ter.  In  some  cases  the  factors  were  common 
to  all  the  systems,  but  in  others  they  differed 
to  a  marked  degree  in  the  respective  systems. 
An  outline  and  comparison  of  the  factors  af 
fecting  the  systems  differently  are  given. 

Composition  of  the  River  Water. 

The  quality  of  the  effluents  in  all  cases  was 
affected  by  the  composition  of  the  river  water, 
on  account  of  the  widely  varying  amounts  of 
chemical  which  were  added  to  the  water  in 
its  various  stages,  as  shown  in  the  foregoing 
summary  of  results  by  periods.  Owing  to  the 
large  quantity  of  suspended  matter  frequently 
present  in  the  river  water,  it  was  necessary  at 
such  times  in  the  case  of  all  the  systems,  to 
add  to  the  water  comparatively  large  amounts 
of  alum  or  sulphate  of  alumina.  As  already 
explained,  such  additions  caused  an  increase 
in  the  corroding  action  of  the  effluents,  due 
to  the  increased  amounts  of  carbonic  acid  gas 
set  free;  and  also  made  the  water  less  desir 
able  for  boiler  use.  owing  to  the  compara 
tively  large  amount  of  lime  changed  from 
carbonate  into  the  form  of  sulphate.  Large 
amounts  of  alum  or  sulphate  of  alumina  did 
not  necessarily  affect  the  quality  of  the  efflu 
ents  in  other  respects,  provided  the  quantity 
was  kept  below  that  which  could  be  decom 
posed  by  the  carbonates  and  bicarbonates 
(alkalinity)  of  the  river  water. 

One  observation  of  much  practical  signifi 
cance,  which  was  repeatedly  noted,  may  be 
recorded  here. 

This  observation  refers  to  the  relation  of 
the  amounts  of  sulphate  of  alumina  necessary 
to  produce  a  perfectly  clear  effluent,  and  that 
necessary  to  give  a  satisfactory  efficiency  to 
the  system  in  the  removal  of  bacteria. 
Early  in  the  investigations  it  was  noted  that 
as  the  composition  of  the  river  water  varied 
from  time  to  time,  the  amounts  of  sulphate 
of  alumina  necessary  to  produce  the  two 


SUMMARY  AND   DISCUSSION  OF  DATA    OF   1895-96. 


25' 


above-named    results,    respectively,   were   far 
from  parallel. 

The  most  marked  examples  of  this  were 
observed  in  March  and  May,  iXgf).  During 
the  latter  days  of  March,  the  suspended  mat 
ter  in  the  river  water  was  comparatively  large 
in  size,  and  of  a  red  color;  and  the  effluents 
in  many  cases  were  clear,  even  brilliant,  with 
out  a  satisfactory  removal  of  bacteria.  Dur 
ing  the  latter  part  of  May,  however,  the  rains 
which  fell  after  a  long  period  of  drought  pro 
duced  such  a  character  of  the  water  in  the 
river,  that  the  suspended  matters  were  very 
light  and  minute.  In  some  cases,  the  sus 
pended  particles  were  finer  than  bacteria  and 
not  more  than  o.ooooi  inch  in  diameter  as 
measured  under  the  microscope. 

Under  these  circumstances  the  appearance 
of  the  effluent  became  unsatisfactory  in  less 
than  one-half  hour  after  the  niters  were  put 
in  service  after  a  thorough  washing,  and 
when  the  number  of  bacteria  in  the  effluent 
remained  normal.  But  the  most  interesting 
observation  made  upon  these  conditions  was 
that  the  effluent  became  unsatisfactory  in  ap 
pearance  before  there  was  a  perceptible  in 
crease  in  the  acting  head  necessary  to  pro 
duce  filtration  at  the  given  rate.  These  effects 
were  evidently  due  to  an  inadequate  degree  of 
coagulation  of  the  water  as  it  entered  the  sand 
layer  to  be  filtered  at  the  given  rate. 
I  ' 
Application  of  Alum  or  Sulphate  of  Alumina. 

Preparation  of  Solutions. — This  question 
was  referred  to  in  general  terms  in  Chapter 
II.  In  the  case  of  the  solutions  of  sulphate 
of  alumina,  with  a  very  few  exceptions,  it  is 
not  probable  that  the  quality  of  the  effluents 
was  affected  by  irregularities  in  their  prepara 
tion.  In  all  cases,  however,  it  would  be  de 
sirable  in  the  operation  of  a  large  system  to 
employ  more  careful  and  systematic  methods 
than  were  noted  at  times. 

The  point  to  which  attention  is  especially 
invited  at  this  time  is  in  connection  with  the 
first  device  used  by  the  Western  Company  for 
the  preparation  of  solutions  of  potash  alum. 
In  winter  weather,  when  the  temperature  of 
the  water  was  low,  the  strength  of  the  solu 
tions,  obtained  by  the  passage  of  a  current  of 
water  through  an  alum  tank  placed  on  a  by 


pass  on  the  main  water-pipe,  was  so  irregular 
that  the  method  may  be  pronounced  a  failure, 
so  far  as  its  application  for  the  coagulation  of 
the  rapidly  changing  Ohio  River  water  is 
concerned.  The  use  of  this  device  was  dis 
continued  by  the  Western  Company  on 
April  <j. 

Uniforinitv  of  Application  of  Solutions. — 
With  regard  to  the  regular  application  of  so 
lutions  of  chemicals  in  suitable  amounts  to 
effect  proper  coagulation  of  the  varying  river 
water,  all  devices  gave  the  appearance  of  be 
ing  crude,  so  far  as  their  part  in  the  produc 
tion  of  a  satisfactory  effluent  was  concerned. 
With  a  water  of  a  certain  grade  the  applica 
tion  of  chemicals  by  the  Warren  device  was 
fairly  satisfactory  on  the  whole.  With  the 
Jewell  and  second  Western  devices  satisfac 
tory  results  could  be  obtained  by  giving  them 
close  attention.  Such  attention,  however, 
was  not  regularly  given  to  them,  especially 
during  the  earlier  part  of  the  investigation. 

In  its  use  during  these  tests  the  first  West 
ern  device  was  a  failure,  even  when  an  attend 
ant  stood  over  it  practically  all  the  time.  Not 
only  did  the  operators  lose  control  of  the  rate 
of  application  of  the  solution,  but,  as  noted 
above,  their  inability  to  control  the  rate  of  ap 
plication  was  increased  by  the  widely  varying 
strength  of  the  chemical  solutions.  In 
warmer  weather  when  the  water  would  dis 
solve  greater  quantities  of  alum  the  operation 
of  the  device  would  be  still  more  unsatisfac 
tory. 

Application  of  Lime. 

Lime  was  applied  to  the  river  water  only  by 
the  Jewell  System.  Under  the  existing  cir 
cumstances  its  application  was  unnecessary. 
The  object  of  its  application  was  apparently 
to  guard  against  the  passage  of  undecom- 
posed  sulphate  of  alumina  into  the  effluent, 
and  perhaps  to  facilitate  the  coagulation  of 
the  water  by  the  regular  chemicals.  The 
trial  of  the  application  of  lime  by  the  Jewe'l 
System  was  followed  by  disastrous  results  so 
far  as  the  quality  of  the  effluent  was  con 
cerned.  This  was  due  chiefly  to  the  manner 
of  application  of  the  lime.  At  times  the  lime 
and  sulphate  of  alumina  must  have  reached 
the  river  water  alternately,  and  produced  of 


WATER   PURIFICATION  AT  LOUISVILLE. 


course  an  effluent  of  unsatisfactory  character. 
At  other  times  the  sulphate  of  alumina  was 
decomposed  in  the  feed  pipe  leading  from  the 
pump  to  the  main  inlet  water-pipe.  After  the 
adoption  of  the  separate  feed  pipes,  shortly 
before  the  abandonment  of  the  use  of  lime, 
the  above  difficulties  were  removed  to  a 
greater  or  less  degree.  In  this  connection 
reference  is  made  to  some  comparative  ex 
periments  upon  the  coagulation  of  the  Ohio 
River  water  by  aluminum  hydrate  under  dif 
ferent  conditions  made  by  the  Water  Com 
pany,  and  recorded  in  Chapter  XII. 

It  is  not  to  be  inferred  from  these  com 
ments  that  the  use  of  lime  would  not  be  ad 
vantageous  for  some  conditions  and  for  some 
waters.  The  above  criticism  refers  only  to  the 
fact  that  its  application  during  these  tests  was 
unnecessary,  and  that  its  manner  of  applica 
tion  in  the  Jewell  System  was  not  well  ad 
vised. 


For  all  the  varying  conditions  of  the  river 
water  there  was  doubtless  a  certain  amount 
of  sulphate  of  alumina,  which,  by  virtue  of  its 
coagulating  power,  was  best  adapted  for  the 
purification  of  the  water  by  each  of  the  sys 
tems.  To  define  this  optimum  amount  for 
any  given  conditions  is  impossible  with  the 
available  data.  Inspection  of  the  records 
and  summaries  shows  that  all  of  the  systems 
were  operated  far  from  this  mark  at  times. 
This  was  more  noticeable  during  the  early 
than  during  the  later  part  of  the  investiga 
tions,  when  the  operators  had  some  experi 
ence  to  guide  them.  It  will  readily  be  seen 
that  the  liberal  use  of  chemical  by  the  War 
ren  and  Jewell  systems  was  reversed  at  times 
during  the  tests.  Comparing  the  effect  of  the 
actual  quantities  used  upon  the  quality  of  the 
effluent  with  that  of  the  optimum,  it  may  be 
stated  that  in  numerous  cases  the  actual 
quantity  appeared  to  be  below  the  optimum, 
and  showed  its  effect  by  high  bacteria  in  the 
effluent,  or  unsatisfactory  appearance,  or 
both.  At  times  the  actual  quantity  was  in 
excess  of  the  optimum,  and  affected  the  ef 
fluent  by  an  unnecessary  increase  in  its  cor 
roding  action  and  capacity  to  form  scale  in 


boilers,  as  already  discussed  in  this  chapter. 
Comments  along  this  line  will  be  found  in  the 
next  section,  under  the  cost  of  applied  chem 
icals.  For  further  information  in  this  con 
nection  reference  is  made  to  the  detailed  data 
in  foregoing  tables. 

Provision  for  the  Removal  of  Suspended  Matter 
from  the  River  Water  by  Sedimentation. 

At  times  of  flood  the  Ohio  River  water 
contains  large  quantities  of  heavy  mud,  and 
experience  indicates  that  in  the  neighbor 
hood  of  75  per  cent,  of  this  mud  on  an  aver 
age  may  be  removed  economically  by  plain 
subsidence  without  the  use  of  coagulating 
chemicals.  At  other  times,  especially  during 
the  spring  and  early  summer,  the  river  water 
contains  large  quantities  of  very  finely  di 
vided  suspended  matter,  which  would  require 
days  and  perhaps  weeks  for  the  removal  of 
the  bulk  of  it  by  plain  subsidence.  The  evi 
dence  presented  in  Chapter  IV,  however,  in 
dicates  that  it  could  be  removed  after 
relatively  short  subsidence,  following  the  ap 
plication  of  comparatively  small  amounts  of 
a  coagulating  chemical. 

In  all  cases  not  only  were  provisions  for 
plain  subsidence  entirely  lacking,  but  the  pe 
riod  for  coagulation  and  subsidence  was  far 
too  short.  Turning  to  the  summaries  of  re 
sults  it  will  be  noted  in  the  case  of  all  the  sys 
tems  that  the  increase  in  applied  chemical, 
due  to  muddy  water,  reached  at  times  as  high 
as  8  grains  per  gallon.  The  effect  of  the  ap 
plication  of  large  quantities  of  chemical,  with 
reference  to  corrosion  and  incrustation,  has 
been  referred  to  above.  With  plain  subsid 
ence  followed  by  longer  periods  of  coagula 
tion  and  subsidence  these  high  amounts  of 
coagulant  could  be  reduced  materially. 
There  are  also  indications  that  at  times  it 
would  be  advisable  to  make  more  than  one 
application  of  coagulant.  The  Warren  Sys 
tem  was  superior  to  the  others  with  regard  to 
provisions  for  the  removal  of  suspended  mat 
ter  from  the  river  water  by  subsidence,  but 
even  in  this  case  the  provisions  were  wholly 
inadequate  to  prevent  the  use  of  excessive 
amounts  of  an  expensive  chemical,  and  their 
attending  effects.  In  fact  this  was  the  weak 
est  feature  of  all  these  svstems. 


SUMMARY  AND  DISCUSSION  OF  DATA    OF   1895-96. 


253 


Provisions  for  Cleaning. — All  of  the  systems 
were  very  weak  in  provisions  for  ready  and 
economical  cleaning  of  the  compartments  in 
which  sedimentation  took  place.  How  far 
this  affected  the  character  of  the  effluent  it  is 
difficult  to  estimate,  as  apparently  these  com 
partments  were  cleaned  in  the  case  of  each  of 
the  respective  systems  at  as  frequent  intervals 
as  was  thought  necessary.  It  is  probable, 
however,  that  the  difficulties  of  cleaning,  due 
to  lack  of  provision  for  the  ready  and  econom 
ical  performance  of  this  operation,  often  led 
to  delay  in  cleaning,  and  to  the  consequent 
passage  of  sludge  from  the  basin  or  chamber 
upon  the  filter. 

Provisions  for  Inspection. — The  need  for 
regular  and  systematic  inspection  of  the  in 
terior  of  the  compartments  in  which  sedimen 
tation  took  place,  and  of  the  contents  of  these 
compartments,  seemed  to  have  been  almost 
wholly  ignored  in  these  systems.  This  was 
especially  true  in  the  case  of  the  Western  Sys 
tems,  where  the  arrangements  were  such  as 
to  necessitate  the  draining  of  the  settling 
chamber,  to  examine  its  contents.  The  fail 
ure  to  inspect  the  condition  of  the  contents  of 
these  compartments,  with  regard  to  the 
amount  or  sludge,  undoubtedly  led  also  to 
delays  in  cleaning  the  compartments,  with 
the  resultant  effect  of  the  passage  of  sludge 
from  the  basin  or  chamber  upon  the  filter.  The 
most  notable  example  of  this  was  found  in  the 
Warren  System  on  July  22-27. 

Degree  of   Coagulation   of   the   Partially   Sub 
sided  Water  as  it  entered  the  Sand  Layer. 

The  degree  of  coagulation  of  the  water  as 
it  entered  the  sand  layer  was  found  to  be  the 
most  important  feature  of  satisfactory  and 
efficient  purification  by  this  type  of  filter.  To 
an  experienced  observer  the  proper  degree 
could  be  told  with  considerable  accuracy  by 
the  size  of  the  Hakes  or  masses  of  coagulated 
material  and  the  rapidity  with  which  they 
subsided.  The  coagulation  had  to  be  thor 
ough;  that  is,  the  volume  of  hydrate  had  to 
be  practically  sufficient  to  envelop  all  sus 
pended  matters  or  furnish  enough  gelatinous 
surface  to  which  the  particles  could  adhere. 
It  is  believed  that  just  after  washing  this  is 
absolutely  true,  but  after  a  filter  had  been  op 


erated  for  a  time  and  flakes  of  coagula  had 
accumulated  in  the  sand  there  might  be  per 
missible  a  slight  departure  from  thorough 
coagulation.  Thorough  coagulation  of  the 
water  above  the  sand,  or  very  nearly  thor 
ough,  was  absolutely  essential  in  order  to  re 
move  the  fine  clay  particles;  and  during  the 
greater  part  of  the  year  the  removal  of  bac 
teria  was  satisfactory  when  the  effluent  was 
free  from  turbidity. 

At  times  during  the  winter,  however,  when 
the  suspended  matter  was  very  coarse  the- 
bacterial  efficiency  required  especial  atten 
tion. 

Taking  everything  into  consideration  it 
may  be  safely  concluded  that  the  volume  of 
available  hydrate  in  the  water  as  it  entered 
the  sand  layer  was  the  most  important  fea 
ture  of  successful  filtration;  and  that  when  the 
amount  of  hydrate  present  departed  materi 
ally  from  that  necessary  for  complete  coagu 
lation  a  uniformly  satisfactory  quality  of  the 
effluent  could  not  be  expected. 

Sand  Layers  of  the  Several  Filters. 

Very  little  information  upon  the  relative 
value  of  each  of  the  more  important  features 
of  the  sand  layers  is  available,  as  was  stated 
to  you  July  n,  1896.  This  is  explained  by 
the  fact  that  a  series  of  factors  unavoidably 
worked  together  to  disguise  the  influence 
of  any  particular  factor.  The  two  principal 
factors  which  affected  the  efficacy  of  the  sand 
layers  in  purifying  the  water  were  the  degree 
of  coagulation  of  the  water  and  the  rate  of  fil 
tration.  Both  of  these  factors  are  referred 
to  in  their  proper  order. 

All  things  considered  the  sand  layers  of  the 
Jewell  System  were  the  most  efficient  in  pro 
ducing-  an  effluent  of  satisfactory  character. 

A  brief  outline  of  the  more  important 
points  as  the  systems  stood  at  the  close  of 
the  tests  is  as  follows: 

Thickness. — The  thickness  of  the  sand  lay 
ers  in  the  respective  systems  was  as  follows: 


Warren 

Jewell 

Western  Gravity. . 
Western  Pressure. 


Inchr 


Z7.O 
30.5 
31.0 
49-5 


254 


WATER  PURIFICATION  AT  LOUISVILLE. 


Although  the  Jewell  sand  layer  gave  the 
best  results  it  is  still  an  open  question  what 
the  thickness  of  the  sand  layer  should  be  to 
give  the  best  results  under  favorable  circum 
stances  with  regard  to  other  conditions. 
The  Western  sand  layers  did  not  appear  to 
advantage,  owing,  it  seems,  to  failure  to  wash 
them  satisfactorily  and  at  times  to  the  degree 
of  coagulation  with  reference  to  the  rate  of 
filtration. 

Size  of  Grain. — A  comparison  of  the  sizes 
•of  the  grains  in  the  several  sand  layers,  as 
shown  by  their  effective  sizes  (10  per  cent. 
of  the  material  finer  than  the  diameter  given 
in  millimeters),  is  as  follows: 


System. 

Effective 
Size. 

Warren 

o.  51 

Jewell 

0.43 

0.43 

Western 

Pressure  

0.44 

The  Warren  material  was  apparently  too 
coarse  to  give  uniformly  the  most  efficient  re 
sults  under  the  existing  conditions.  The  fine 
material  of  the  two  Western  systems  was 
mixed  in  both  cases  with  very  coarse  sand, 
giving  the  resultant  layer  a  rather  higher  ef 
fective  size.  These  mixed  sands  were,  how 
ever,  as  fine  in  effective  size  as  that  of  the 
Jewell,  but  their  use  wa's  handicapped  by  fac 
tors  mentioned  under  Thickness  of  Sand  Layer. 

Composition. — The  available  evidence,  so 
far  as  it  goes,  points  to  as  satisfactory  results 
under  suitable  conditions  from  natural  sands, 
of  uniform  and  proper  size,  as  from  the  more 
expensive  crushed  quartz. 

Rate  of  Filtration. 

Unless  some  abnormal  and  disturbing  fea 
tures  appeared,  the  rates  of  filtration  were 
maintained  so  as  to  give  as  nearly  as  possible 
the  contract  capacity  of  250,000  gallons  per 
24  hours  for  each  system.  At  times  of  very 
muddy  water  none  of  the  systems  reached  the 
(  prescribed  amount,  owing  to  the  incomplete 
preliminary  subsidence.  The  rates  differed 
somewhat  in  the  different  systems,  due  for 
the  most  part  to  the  different  areas  of  the 
sand  layers  in  relation  to  the  contract  rate. 
As  a  rule  the  rates  were  held  fairly  uniform 
under  the  same  conditions  of  river  water,  the 


range  of  variation  under  parallel  conditions 
being  usually  less  than  10  per  cent.  The 
widely  varying  factors  which  influenced  the 
results  at  different  times  in  addition  to 
changes  in  rate  prevent  the  drawing  of  any 
specific  conclusions. 

In  the  following  table  are  given  the  rates 
in  million  gallons  per  acre  daily,  the  amounts 
of  suspended  solids  in  the  river  water  in  parts 
per  million,  the  amounts  of  sulphate  of  alu 
mina  used,  in  grains  per  gallon,  and  the  bac 
terial  efficiencies  of  the  several  systems,  for 
those  runs  on  which  the  unit  rates  were  the 
maximum  and  the  minimum,  and  also  the 
average  of  these  quantities  for  the  entire  in- 


TABLE  OF  LEADING  RESULTS  WITH   MAXIMUM 
AND    MINIMUM    UNIT   RATES,   AND   AVERAGE 
RESULTS  FOR  THE  ENTIRE  INVESTIGATION. 

WAKRKN 

JEWELL. 

Min. 

Max. 

Aver. 

Min. 

Max. 

Aver. 

Rate  7 

80 
1677 

7.92 
97-5 

155 
36 

0.98 
95.2 

120 

2.70 
96.7 

57 
2OO 

2.01 

95-7 

150 
220 

5-50 
99.9 

100 

2.49 
96.0 

Sulph.  of   alu 
mina  
Bacterial     effi 
ciency  

WKSTKRN  GRAVITY. 

WBSTBRN  PKESSUHE. 

•    Min. 

Max. 

Aver. 

Min. 

Max. 

Aver. 

Rate  

33 
420 

9-33 
99.0 

152 
17 

o.  71 
92.6 

96 

83 

202 

154 

Sulph.  of   alu 
mina  
Bacterial     effi 
ciency  

2.90 
97-4 

91.4 

1.24 
96.8 

2.41 
97-3 

As  stated  above,  the  wide  variations  in  the 
controlling  factors  make  it  practically  impos 
sible  to  draw  any  definite  conclusions  from  the 
results  in  regard  to  the  relative  efficiencies 
of  different  unit  rates.  That  within  the 
ranges  employed,  the  lower  rates  did  not  give 
uniformly  any  better  results  than  the  higher 
ones,  and  that  the  maximum  limits  of  safe 
rates  were  not  reached  in  this  work  is  indi 
cated  by  the  results  of  the  last  table  and 
clearly  shown  by  the  next  table.  In  this 
table  are  given  averages  of  the  leading  results 
of  the  Warren  and  Jewell  systems,  omitting 
Periods  Nos.  i  and  2.  These  averages  have 
been  arranged  with  regard  to  the  unit  rates 
in  order  to  allow  comparison  of  the  results 
from  this  standpoint.  In  the  case  of  the 
Western  Systems  the  degree  of  coagulation 


SUMMARY  AND   DISCUSSION  OF  DATA    OF   1895-96. 


255 


and  other  factors  were  too  irregular  for  these 
systems   to   be   given   a  place   in   this   table. 


The  headings  and  results  have  a 
and  explained  before. 


been  used 


LEADING    AVERAGE    RESULTS    OF    THE   WARREN    AND  JEWELL   SYSTEMS,    ARRANGED 
ACCORDING    TO    UNIT    RATES    OF    FILTRATION. 

Warren  System. 


Rates  included  in  averages  

80-89 

90-99 

46 

IOO-IO9 
69 

IIO-II9 

120-129 

130-139 

58 

140-149 

Rates  in  million  gallons   per  acre  per 
24  hours  .... 

86  5 

Amounts  of  suspended  solids  in  river 

526 

258 

Amounts  of   applied   sulphate   of  alu- 

4  46 

4  IS 

<!     87 

2.8o 

Amounts  of  water  filtered  per  run  in 

2  868 

5  660 

Percentages  which   the  water  used  for 
washing    and    wasted    was    of    the 

Bacterial  Efficiencies  

98.0 

98.4 

98.2 

99.1 

97-9 

98.9 

98-5 

Jewell  System. 


Rates  included  in  averages  

80-89 

90-99 

100-109 

I  IO-II8 

119-130 

138-143 

76 

18 

8 

Rates   in  million  gallons   per  acre  per 

85  o 

Amounts  of  suspended  solids  in  river 

water  in  parts  per  million  

1310 

59i 

220 

476 

458 

278 

Amounts   of   applied  sulphate  of  alu 

mina  in  grains  per  gallon  

5.80 

3-9° 

2.88 

3-85 

3-95 

5.06 

Amounts  of  water  filtered   per  run   in 

Percentages  which  the  water  used  for 

washing    and    wasted    was    of    the 

18 

16 

Bacterial  efficiencies  

97-3  ; 

98.0 

97.6 

98.7 

98.6 

99.2 

These  data  show  conclusively  that  within 
these  limits  in  rate  of  filtration  and  under  the 
given  conditions  there  were  other  factors  of 
more  practical  significance  than  the  rates  of 
flow  through  the  sand.  Unquestionably,  the 
most  prominent  of  these  factors  was  the  de 
gree  of  coagulation  of  the  water  as  it  entered 
the  sand  layer. 

How  high  it  would  be  possible  or  practic 
able  to  carry  the  rate  of  nitration  in  efficient 
and  economical  purification  by  this  method 
cannot  be  stated  at  present;  and  it  would  re 
quire  for  its  proper  solution  conditions  where 
the  bulk  of  the  suspended  matters  was  removed 
by  subsidence.  Some  data  showing  the  in- 
advisability  of  employing  rates  of  less  than 
100  million  gallons  per  acre  daily  were  ob 
tained  in  1897,  and  are  recorded  in  Chap 
ter  XV. 

Regulation    and   Control   of   Operation    of   tlic 
Pilfers. 

While  considerable  care  was  necessary  in 
the  operation  of  the  niters  in  order  to  secure 


a  satisfactory  effluent  it  was  very  seldom  that 
moderate  irregularities  in  the  rate  of  filtration 
made  their  influence  apparent.  The  pres 
ence  of  certain  irregularities  in  the  pressure 
or  acting  head  upon  the  Western  pressure 
filter  was  found  to  be  a  very  disturbing  and 
disastrous  element,  and  as  a  rule  caused  fil 
tration  to  be  stopped  and  the  filter  washed. 

Loss  of  Head. 

As  the  frictional  resistance  to  the  passage 
of  water  of  the  sand  layers  and  their  accumu 
lation  increased,  the  necessary  acting  head,  or 
loss  of  head,  increased  and  approached  tow 
ards  the  maximum  available  head.  The  sev 
eral  filters  behaved  quite  differently  in  this 
respect.  The  Warren  filter  contained  a  coarse 
sand  layer  and  almost  without  exception  the 
appearance  and  quality  of  the  effluent  became 
unsatisfactory  when  the  loss  of  head  was 
much  less  than  the  total  available  head.  As 
a  rule  the  filter  of  the  Warren  System  was 
washed  when  the  loss  of  head  was  less  than 
3  feet. 


WATER   PURIFICATION  AT  LOUISVILLE. 


During  a  large  part  of  the  time  the  Jewell 
System  employed  the  full  available  head 
(12-14  feet)  ou  their  filter  before  the  sand 
layer  was  washed,  although  it  is  to  be  noted 
that  the  last  two  feet  of  head  (from  10  to  12 
feet)  were  not  of  great  value  as  the  resistance 
increased  very  rapidly  above  10  feet.  This 
was  not  always  possible,  however,  especially 
when  the  coagulation  of  the  water  as  it  en 
tered  the  filter  from  the  settling  chamber  was 
incomplete.  This  factor  was  also  a  very  im 
portant  one  in  connection  with  the  employ 
ment  of  surface  agitation  during  the  runs. 
From  the  detailed  data  in  Chapter  VIII,  it 
will  be  noted  that  in  many  instances  this  op 
eration  was  successfully  used  in  the  Jewell 
System. 

In  the  Western  Gravity  System  the  filter 
was  washed  because  the  loss  of  head  reached 
the  maximum  in  the  case  of  the  Western 
gravity  filter  (A),  and  in  very  few  cases  did 
the  quality  or  appearance  of  the  effluent  de 
teriorate  as  the  loss  of  head  increased.  The 
opposite  of  this  was  uniformly  true  in  the 
case  of  the  Western  gravity  filter  (B). 

Frequent  ''  breaks "  were  noted  in  the 
Western  pressure  filter  when  the  loss  of  head 
was  a  small  fraction  of  the  available  head, 
which  was  equal  approximately' to  the  pres 
sure  in  the  force  main  to  the  reservoir.  These 
breaks,  evidently  due  for  the  most  part  to  ir 
regularities  in  pressure,  causing  the  water  to 
pass  through  some  channel  or  place  of  les 
sened  resistance  at  an  abnormal  rate,  caused, 
in  turn,  the  effluent  to  become  turbid,  and 
necessitated  washing  the  filter.  Previous  to 
June  i,  this  filter  was  operated  with  widely 
varying  maximum  acting  !heads,  the  appar 
ent  custom  being  to  wash  at  from  30  to  50 
feet  loss  of  head,  unless  the  effluent  showed 
deterioration.  After  this  date  the  practice 
was  changed.  20  feet  being-  apparently  adopt 
ed  as  a  maximum.  It  was  seldom,  however, 
that  more  than  15  feet  of  acting  head  were 
employed,  and  as  a  rule  it  was  found  advisa 
ble  to  wash  the  filter  when  the  loss  of  head 
was  less  than  10  feet. 

With  a  water  which  contained  such  a  large 
amount  of  very  finely  divided  suspended  mat 
ter,  as  was  the  case  during  the  last  days  of  May, 
all  the  filters  gave  a  poor  effluent  before  there 
was  any  marked  increase  in  'the  loss  of  'head, 
as  already  noted. 


There  were  no  well-marked  indications  that 
there  was  any  difference  in  the  action  of  the 
negative  head  of  the  Jewell  filter,  as  com 
pared  with  the  positive  head  of  the  other  fil 
ters. 


By  some  the  belief  has  been  held  that  just 
after  washing  filters  of  this  type,  the  effluent 
is  of  an  unsatisfactory  character,  and  that  it  is 
necessary  to  waste  the  first  portion  of  the  fil 
tered  water.  One  of  the  most  important 
points  learned  in  these  tests  was  that  such 
was  not  necessarily  the  case,  provided  the 
sand  layer  was  thoroughly  washed  and  the 
applied  water  sufficiently  coagulated.  As  a 
rule  the  sand  layers  in  the  Warren  and  Jewell 
systems  were  washed  quite  thoroughly,  but 
more  especially  and  uniformly  so  in  the  case 
of  the  Warren;  and  it  was  very  rare  during 
the  later  part  of  the  tests  that  the  first  por 
tion  of  these  effluents  after  washing  was  in 
ferior  in  appearance  or  character  to  the  re 
maining  portions.  In  connection  with  this 
important  and  practical  point  it  is  to  be  noted 
that  both  of  the  above  systems  employed  con 
stant  agitation  of  the  sand  layer  during  wash 
ing.  The  sand  layers  of  both  of  'these  systems 
were  usually  washed  until  the  filtered  water, 
which  was  pumped  into  them  from  below  the 
sand  layer,  was  comparatively  clear  as  it  over 
flowed  from  the  filter  above  the  sand. 

All  of  the  systems  regularly  employed  fil 
tered  water  for  washing  the  sand  layer  during 
these  tests,  except  in  the  case  of  the  Western 
Systems  from  June  24  to  July  27,  inclusive, 
when  river  water  was  used  by  these  two  sys 
tems.  From  the  fact  that  the  operators  of  the 
Western  Systems  abandoned  the  use  of  unfil- 
tered  water  for  washing  it  may  be  inferred 
that  its  use  was  not  wholly  satisfactory. 

One  reason  why  the  Western  Systems  tried 
the  use  of  unfiltered  water  for  washing,  ap 
parently,  was  that  it  was  their  uniform  custom 
to  waste  the  first  portion  of  effluent  after 
washing  the  sand  layer.  It  seems  very  clear 
that  this  was  required  partly  by  incomplete 
washing  and  partly  by  incomplete  coagula 
tion  of  the  applied  water.  Several  factors  af 
fected  the  thoroughness  of  washing  the  sand 
layers  of  these  filters.  The  most  important 
one  was  the  absence  of  accompanying  agita- 


SUMMARY  AND   DISCUSSION   OF  DATA    OF   .895-96. 


257 


tion.  Another  important  one  was  the  unsat 
isfactory  device  used  for  the  distribution  of 
the  wash-water  beneath  the  sand  layer.  As 
already  described  in  Chapter  V,  this  was  ac 
complished  by  means  of  slotted  brass  tubes, 
which  also  served  for  the  collection  of  the 
effluent  when  the  niters  were  in  service. 
These  slots  were  wedge  shaped,  with  the 
smallest  width  on  the  outside  forming  the 
opening.  It  was  expected  that  by  this  ar 
rangement  the  openings  would  not  clog 
up,  but  that  any  matters  small  enough  to 
lodge  in  them  would  pass  through.  This  was 
in  a  measure  found  to  be  true  at  first,  but  as 
comparatively  large  numbers  of  sand  grains 
passed  through  the  slots  the  thin  edges  soon 
became  worn,  resulting  in  the  passage 
through  of  more  grains  or  in  their  lodgment 
in  the  opening. 

When  the  flow  of  water  was  reversed  dur 
ing  washing,  some  of  the  sand  grains  in  the 


tubes  were  doubtless  forced  into  the  beveled 
openings  and  obstructed  the  Mow.  When 
these  strainer  tubes  were  removed  about  the 
first  of  April  many  of  them  were  found  to  be 
one-third  full  of  sand.  This  state  of  affairs 
naturally  caused  the  sand  layer  to  be  incom 
pletely  washed,  especially  in  the  absence  of 
agitation. 

The  ball  nozzles  which  were  used  for  the 
distribution  of  wash-water  in  the  West 
ern  gravity  filter  (B),  after  the  above  ex 
perience  with  the  slotted  brass  tubes,  did  not 
at  the  outset  possess  the  action  for  which 
they  were  designed.  This  filter  in  its  modi 
fied  form  was  not  operated  long  enough  to 
demonstrate  the  practicability  of  these  de 
vices. 

Sand  samples  from  the  various  filters  were 
collected  from  time  to  time  and  analyzed 
chemically  and  bacterially  with  the  following 
results: 


RESULTS   OF   CHEMICAL    AND    BACTERIAL   ANALYSES   OF  SANDS   OF  THE    RESPECTIVE  SYSTEMS. 

Nitrogen  in  the  form  of  Albuminoid  Ammonia  expressed  in  Parts  per  Million  by  weight  of  dry  Sand. 
Bacteria  expressed  in  Numbers  per  Gram  of  dry  Sand. 


Depth  below  Surface. 

0-0.25  Inch. 

i  Inch. 

Nitro-i  Bac- 
gen.   jteria. 

3  Inches. 

6  Inches. 

12  Inches. 

24! 

flics. 

Bot  of  Layer. 

Date.                     System. 

Nitru- 
gen. 

Bacteria. 

Nitre- 
(fen. 

,££-. 

Nii.ro 
Ren. 

Bac- 

Nitro 

Bac- 

Nitro- 
«en. 

Bac- 

Nitro-.j,     .   ri 
gen.  !    ' 

Before   Washing. 

1896 

Jan.  20:  Warren. . 

May  22 

July  17 

Jan.     8i  Jewel 

Feb.  28 

July    81 

Jan.  i6|  Weste 

July  251 

Jan.  12!  Weste 

June  13 

July  14 


i  Gravity  .... 

26.0 
So.c 
38.8 
365.0 
45.0 
73-3 
171.5 

65  too 
44  Soo 

20.  o 

12.0 

9.0 
11.  8 

6.0 

31  5«o 

7.6 

S.o 

35500 

3-4 

12  600 

1.  9 

56.8 

21  .6 

17.6 

9-6  

6.0 

1  26  (XX) 

;;;, 

6.3 

21  OOO 

2..1 

14  700 

2-7 

452  ooo 

i  Pressure  .  .  . 

100.8 
114.2 

870000 

6.1 
14-4 

9  600 

8-5 

9.6 
n  r> 

IIIOOO 

13-4 

II  .2 

21    IOO 

80.5 

23.6 

IIO.O 

43  7"° 

t 

vfter  Was 

.  .  .  .     16.3  26  ioo    .... 
thing- 

M.7 

27300 

I5.2i     46700 

14  Soo 

"  V'oo 

2.0 
4 

13.4* 

# 

28  S* 

* 

| 

2.4 

2     1* 

# 

* 

4-1 

1     ' 

1   " 

I  800 

Gravity  

2-;.  8 

n   5 

5   s 

Pressure  ...       1  1  .  <; 

TO  ?OO 

8.8 

5  &>-> 

0-0 

After  steaming  the  sand.      Sand  was  practically  sterile. 


WATER   PURIFICATION   AT  LOUISVILLE. 


Relation  of  Proper  Attention  to  the  Efficiency  of 
Purification  of  the  Ohio  River  Water 

by  this  Method. 

'J  his  subject  was  touched  upon  in  Chapter 
VII,  where  the  manner  of  operation  of  the 
several  systems  was  outlined.  In  connection 
with  the  factors  which  exerted  an  appreci 
able  influence  on  the  quality  of  the  filtered 
water,  this  one  must  be  clearly  borne  in  mind. 
The  impression  which  some  people  have  that 
large  systems  of  water  purification  by  this 
method  will  at  all  times  yield  an  effluent  of 
satisfactory  character  with  merely  nominal 
attendance  is  wholly  incorrect  so  far  as  the 
Ohio  River  water  is  concerned.  In  the  first 
place  both  efficiency  and  economy  require 
that  very  close  attention  be  given  to  the  ap 
plication  of  chemicals.  Setting  aside  the 
question  of  cost,  any  excess  of  the  chemical 
above  the  optimum  is  attended  with  increased 
amounts  of  corroding  and  incrusting  con 
stituents  in  the  filtered  water,  and,  under  un 
skilled  supervision,  chemical  in  excess  of  the 
amount  whidh  the  water  will  decompose 
might  be  added  at  times,  resulting  of  course 
in  the  inadmissible  presence  of  imdecomposed 
chemical  in  the  effluent.  On  the  other  hand 
a  reduction  of  the  amount  of  chemical  by  a 
small  percentage  below  the  optimum  would 
cause  immediate  deterioration  in  the  charac 
ter  of  the  effluent,  a  deterioration  which  at 
times  could  not  be  determined  for  several 
days,  as  in  the  case  of  the  Ohio  River  water 
a  clear  effluent  is  not  necessarily  a  pure  efflu 
ent,  especially  during  the  winter  months. 

It  will  be  seen,  therefore,  that  the  efficiency 
of  filtration  requires  very  close  adherence  to 
the  optimum  amount  of  chemical  treatment, 
a  problem  which  is  very  difficult  of  solution 
in  the  present  state  of  the  art,  and  the  solu 
tion  of  which  by  unskilled  hands  is  absolutely 
out  of  the  question.  Among  the  many  other 
different  factors  which  affect  the  quality  of 
the  effluent  and  which  are  to  a  greater  or  less 
degree  dependent  on  the  character  of  the  at 
tendants  for  their  efficiency  may  be  men 
tioned  the  following:  The  decision  to  wash  the 
sand  layer,  the  process  of  washing,  the  opera 
tion  of  the  many  mechanical  devices,  and 
finally  the  general  supervision  and  systematic 
methods  of  procedure  without  which  no  sys 
tem  of  this  kind  can  be  successful. 


With  adequate  facilities  for  the  removal  of 
the  coarse  matter  by  plain  subsidence  the 
amount  of  attention  for  successful  operation 
would  be  largely  reduced,  because  it  would 
make  the  water  just  prior  to  its  filtration 
much  more  uniform  in  character. 

SECTION  No.  3. 

PROMINENT  FACTORS  WHICH  INFLUENCED 
THE  ELEMENTS  OF  COST  OF  PURIFICA 
TION  OF  THE  OHIO  RIVER  WATER  IN 
THE  CASE  OF  THE  RESPECTIVE  SYSTEMS. 

The  factors  which  will  be  considered  in  re 
lation  to  the  elements  of  cost  are  substan 
tially  the  same  as  those  noted  in  the  last  sec 
tion  with  regard  to  the  quality  of  the  efflu 
ents.  In  many  respects  the  t\vo  sections 
should  be  considered  side  by  side. 

In  the  following  pages  of  this  chapter  com 
parisons  are  made  of  the  different  factors  as 
they  were  found  at  times  of  fairly  clear  and 
muddiest  water  and,  so  far  as  possible,  under 
normal  conditions,  respectively. 

For  this  purpose  averages  are  used  as  fol 
lows:  For  fairly  clear  water,  averages  during 
Period  No.  13;  for  muddiest  water,  averages 
during  Period  No.  20,  excluding  those  runs 
which  were  affected  by  the  period  of  sub 
sidence  over  night  or  Sunday  ;  for  normal 
water  in  most  cases,  averages  for  the  entire 
investigation.  When  the  Western  Gravity 
System  is  referred  to,  Periods  Nos.  8  and  9 
are  used  in  place  of  Periods  Nos.  13  and  20. 

It  must  be  borne  in  mind  that  the  averages 
as  obtained  above  do  not  represent  the  con 
ditions  as  they  would  exist  under  the  actual 
times  of  muddiest  water  in  the  Ohio  River, 
but  they  are  taken  as  the  best  figures  obtained 
during  the  investigation,  and  as  sufficiently 
marked  to  illustrate  the  points  under  discus 
sion. 

Composition  of  the  River  Water. 

Inspection  of  the  records  for  the  several 
periods  shows  clearly  that  the  amount  of  sus 
pended  matter  in  the  water  exerted  a  marked 
influence  upon  the  cost  for  the  chemical.  The 
extreme  quantities  of  sulphate  of  alumina  ap 
plied  to  the  river  water  were  12.60  and  0.40 


SUMMARY  AND   DISCUSSION  OF   DATA    OF    1895-96. 


2S9 


grains  per  gallon  of  applied  water.  At  1.5 
cents  per  pound  this  would  make  on  this  basis 
the  daily  cost  for  the  chemical  in  the  operation 
of  a  plant  of  25,000,000  gallons  daily  capacity 
range  from  $678  to  $21  by  these  systems. 

The  above  figures,  however,  do  not  show 
the  full  influence  exerted  by  the  composition 
of  the  river  water  upon  the  cost  of  chemical 
in  purification  by  this  system.  When  the 
river  water  was  comparatively  clear  the  aver 
age  percentages  of  applied  water  which  was 
wasted  and  used  for  washing  the  sand  layers 
in  the  Warren,  Jewell,  Western  Gravity  and 
Western  Pressure  systems  were  6,  2,  9,  and 
4,  respectively.  When  the  water  was  in  its- 
muddiest  condition  these  average  percentages 
became  34,  25,  99,  and  58,  respectively. 

In  view  of  the  fact  that  the  evidence  indi 
cates  that  the  Western  Gravity  System  (A) 
was  unable  at  times  of  muddiest  river  water 
to  purify  enough  water  to  wash  its  own  sand 
layer  properly,  and  that  the  data  in  regard 
to  the  Western  Gravity  System  (B)  are  not 
sufficiently  extended  to  permit  the  drawing 
of  any  comparisons,  these  systems  will  be 
omitted  from  further  comparisons  at  this 
time.  As  will  be  seen  by  inspection  of  Table 
Xo.  4,  and  of  the  tables  in  Chapter  VIII, 
where  the  full  records  are  presented,  the 
amounts  of  wash  and  waste  water  in  the  case 
of  the  Jewell  and  Western  Pressure  systems, 
exceeded  at  times  TOO  per  cent,  of  the  filtered 
water.  The  contiguous  records  indicate,  how 
ever,  that  these  results  were  abnormal  and 
not  likely  to  occur  under  regular  conditions 
of  practice. 

Figuring  the  amount  of  applied  chemical 
upon  the  average  quantity  of  net  purified 
water,  the  following  range  of  daily  cost  for 
the  chemical  for  the  purification  of  25,000,000 
gallons  of  Ohio  River  water  is  obtained: 


System. 

Daily  Net  Capacity  in  Gallons. 

By  Contract. 

With 
Clear  Water. 

With 

Muddiest 
Water. 

Warren    

250  ooo 
250000 
250000 

2OO  OOO 

266  ooo 
238  ooo 

1  2O  OOO 

160  ooo 
64  ooo 

Western  Pressure  

'  System. 

Daily  Cost. 

Minimum. 

Maximum. 

Warren  

$So 
06 

*547 

584 

filfl 

Jewell    

Western  Pressure... 

From  the  above-stated  increased  per 
centages  of  water  wasted  and  used  for  wash 
ing  at  times  of  muddy  river  water,  it  follows 
that  the  appliances  and  their  operation,  for 


supplying  this  increased  amount  of  water, 
would  be  factors  in  the  cost  of  purification. 
It  is  to  be  noted,  however,  that  under  suitable 
arrangements,  water  which  was  wasted  either 
before  or  after  purification,  might  be  purified 
subsequently.  Water  which  was  used  for 
washing  the  sand  layers,  however,  would 
probably  have  to  be  discharged  into  the 
sewer. 

The  composition  of  the  river  water,  with 
regard  to  its  suspended  matter,  influenced  the 
cost  of  purification  by  reducing  the  net 
capacity  of  the  respective  systems.  This  is 
shown  by  the  following  table,  in  which  the 
actual  average  net  capacities  of  each  system 
as  operated,  is  recorded  in  gallons  per  24 
hours  at  times  of  clear  and  muddiest  water. 


The  above  data  indicate  the  size  of  the  re 
serve  portion  of  the  respective  systems  which 
would  be  necessary  in  order  to  obtain  the  full 
quantity  of  purified  water  when  the  river  was 
in  the  muddiest  condition,  as  shown  by  these 
tests.  They  do  not  indicate  an  adequate  re 
serve  portion  for  all  conditions,  because 
the  Ohio  River  water  contains  at  times  more 
mud  than  was  the  case  in  any  instance  dur 
ing  the  tests  of  these  filters. 


Kind  of  Chemical. — Since  sulphate  of  alu 
mina  on  an  average  contains  about  60  per 
cent,  more  available  alumina  than  potash 
alum,  and  the  two  chemicals  are  of  approxi 
mately  equal  cost,  the  former  is  cheaper  than 
the  latter  in  the  ratio  of  about  16  to  10. 

Preparation  of  Solutions. — On  the  grounds 
of  cost  alone  the  preparation  of  chemical  so 
lutions,  in  the  process  of  application,  should 
receive  fully  as  much  attention  as  was  the 
case  in  these  tests.  In  sojne  instances  econ 
omy  demands  more  care  in  this  particular 
than  was  regularly  given  to  it  in  each  of  the 
systems.  The  chief  point  in  this  connection, 


WATER   PURIFICATION   AT  LOUISVILLE. 


however,  is  to  record  the  failure  of  the  first 
Western  device  to  yield  solutions  of  even  ap 
proximately  uniform  strength,  such  as  econ 
omy  demands  in  the  treatment  of  the  Ohio 
River  water  in  its  rapidly  changing  condi 
tions. 

Method  ami  Uniformity  of  Application. — ir 
regularities  in  the  application  of  the  chemical 
were  frequently  so  marked  that  they  would 
affect  the  cost  of  operations  on  a  large  scale. 
They  were  more  noticeable  during  the  early 
part  of  the  tests,  before  the  operators  of  the 
respective  systems  were  cautioned  on  this 
point  in  an  official  communication  dated 
March  16,  1896,  in  which  among  other  points 
their  attention  was  called  to  such  irregulari 
ties. 

The  \Yarren  device  was  more  satisfactory 
than  the  others,  all  things  considered,  because 
it  was  most  nearly  automatic.  It  had  several 
crude  features,  however,  and  it  is  by  no  means 
clear  that  its  use  would  be  thoroughly  satis 
factory  in  a  large  system. 

The  Jewell  and  second  Western  devices 
were  satisfactory  provided  they  received  suf 
ficient  attention.  At  different  times  during- 
the  same  day  afid  with  the  same  water  the 
rate  of  application  varied  several  fold.  This 
means  that  if  the  minimum  rate  of  application 
was  sufficient  for  its  purpose  the  higher  rates 
caused  a  waste  of  chemical  equal  to  their 
excess  over  the  minimum.  It  may  be  noted 
that  the  use  of  sufficient  chemical  to  insure 
proper  coagulation,  and  a  sufficient  amount 
of  aluminum  hydrate  in  the  water  as  it  passes 
onto  the  sand  layer,  are  absolutely  essential 
for  the  success  of  this  method  of  purification, 
and  that  the  use  of  an  insufficient  amount  of 
chemical  is  out  of  the  question.  To  do  this 
on  a  large  scale  with  the  devices  submitted 
for  investigation  would  be  less  easy  than 
would  be  thought  at  first  to  be  the  case. 

The  first  device  of  the  Western  Company 
for  the  application  of  chemical  was  a  failure 
as  operated  at  the  beginning  of  these  tests; 
and  it  was  abandoned  shortly  after  the 
official  communication  of  the  Water  Com 
pany  on  March  16.  as  mentioned  above. 

The  cost  of  power  for  the  application  of 
the  chemical  depends  of  course  on  the.metho'l 
of  application  used  and  the  strength  of  solu 
tions,  but  with  anv  of  these  devices  it  would 


be  comparatively  insignificant.  With  the 
Warren  device  the  power  would  be  practically 
only  that  required  to  lift  the  chemicals  and 
water  to  the  mixing  tanks.  The  first  Western 
device  required  substantially  no  increase  in 
power  over  that  required  for  handling  the 
river  water.  The  Jewell  and  the  second  West 
ern  devices  both  involved  the  pumping  of  the 
solution  against  the  full  pressure  in  the  mains. 
Assuming  an  average  percentage  strength  of 
one  per  cent,  and  an  average  amount  of 
chemical  of  2.50  grains  per  gallon,  and  that 
the  necessary  water  and  the  chemical  were  de 
livered  on  the  level  of  the  main  house  tloor, 
the  approximate  amount  of  power  required 
on  a  basis  of  25,000,000  gallons  per  24  hours 
would  be  in  each  case  as  follows: 

Warren  System 0.4  H.P. 

Jewell   System 4.0  H.P. 

Western  Press.  System.    4.0  H.P.  (2(1  device) 

In  the  case  of  the  Warren  device  a  very 
small  amount  of  power  was  used  in  turning 
the  propeller  wheel  which  operated  the 
chemical  pump.  The  power  thus  used  was 
probably  only  a  very  small  fraction  of  the 
total  power  used  in  the  application  of  the  so 
lutions,  and  was  furnished  by  the  velocity 
pressure  in  the  water  supply  pipe. 


The  principal  element  of  cost  of  purifica 
tion  of  the  Ohio  River  water  by  this  method 
would  be  the  sulphate  of  alumina  used  for 
coagulation.  That  is  to  say.  this  element 
would  exceed  any  other  one.  including  the 
interest  on  the  cost  of  construction  of  the 
system.  The  cost  for  sulphate  of  alumina 
would  of  course  be  proportional  to  the 
amount,  and  the  amount  used  would  depend 
upon  a  series  of  factors,  of  which  the  follow 
ing  are  the  most  important: 

1.  Composition  of  river  water,  with  regard 
to  the  quantity  and  character  of  suspended 
matter. 

2.  The    optimum    quantity    of    coagulant 
under  the  given  conditions.     The  chief  vari 
able  factor  affecting  this  was  the  composition 
of  the  river  water,  and  the  chief  fixed  factor 
was  the  period  of  coagulation  and  sedimenta- 


SUMMARY  AND  DISCUSSION  OF  DATA    OF   1895-96. 


tion.  In  practice  plain  sedimentation  should 
precede  coagulation,  and  reduce  the  required 
amount  of  coagulant. 

3.  Relation  of  the  actual  to  the  optimum 
quantity  of  applied  chemical  necessary  to 
secure  the  proper  degree  of  coagulation  in 
the  water  during  and  after  subsidence. 

A  brief  discussion  of  the  several  factors  will 
be  found  in  this  chapter  in  their  logical  or 
der. 

Application  of  Lime. 

The  application  of  lime  as  tried  in  an  ex 
perimental  way  by  the  Jewell  System  in 
creased,  apparently,  the  cost  of  proper  treat 
ment,  disregarding  the  cost  of  the  lime  itself, 
because  it  seemed  to  diminish  the  coagulating 
power  of  the  resulting  aluminum  'hydrate. 

Under  other  and  better  conditions  of  ap 
plication  this  might  not  be  the  case.  In  this 
connection,  see  the  results  of  comparative  ex 
periments  recorded  in  Chapter  XII,  on  the 
coagulating  power  of  aluminum  hydrate  pre 
pared  in  several  different  ways. 

Provisions  for  Coagulation  and  Sedimentation. 

In  relation  to  the  quality  of  the  effluent  it 
was  indicated  that  in  this  respect  all  of  the  sys 
tems  were  very  weak,  although  the  Warren 
was  least  so.  When  it  comes  to  a  question  of 
cost  this  weakness  of  all  the  systems  in  their 
present  form  would  make  their  adoption  ex 
pensive  to  an  unnecessary  degree,  and  there 
fore  of  questionable  admissibility.  The 
merely  nominal  period  of  subsidence  with 
coagulation  in  the  Jewell  and  Western  sys 
tems,  and  for  one  hour  or  less  in  the  \Varren 
System,  and  with  no  plain  subsidence  in  any 
case  to  remove  coarse  matter,  materially  in 
creases  the  cost  of  purification  as  follows: 

1.  It  increases  the  cost  for  chemical. 

2.  It  necessitates  a  reserve  portion  of  the 
system  with  all  appurtenances  to  handle  the 
water  when  in  its  muddiest  condition. 

3.  It  necessitates  the  waste  of  an  unusually 
large  amount  of  filtered  water  for  the  purpose 
of  washing  the  sand  layers. 

4.  The  increase  of  water  wasted  as  indi 
cated  above  increases  the  amount  of  water  to 
be  pumped,  and  therefore  the  aggregate  cost 
of  pumping. 


5.  The  use  from  time  to  time  of  a  compara 
tively  large  reserve  portion  of  the  system 
would  require  the  constant  employment  of  a 
full  set  of  trained  attendants,  capable  of  op 
erating  the  entire  system.  This  would  be 
necessary  because  the  freshets  in  the  Ohio 
River  frequently  appear  in  a  most  irregular 
and  unexpected  manner. 

Inspection  of  the  records  of  the  freshets  in 
the  Ohio  River  during  the  past  thirty-five 
years,  presented  in  Chapter  1,  shows  that 
during  many  years  the  river  was  in  a  state  of 
flood  for  longer  and  more  frequent  periods 
than  was  the  case  during  these  investigations. 
This  means  that  in  many  cases  the  river  water 
contained  more  suspended  matter  than  was 
encountered  during  these  tests,  and  there 
fore  the  five  factors  of  cost  stated  above 
would  be  correspondingly  increased. 

In  this  connection  it  is  not  to  be  forgotten 
that  the  Western  Gravity  System  as  first  de 
signed  was  voluntarily  taken  out  of  service 
by  the  Western  Filter  Company  on  March  21, 
because  it  wras  unable  to  yield  enough  filtered 
water  to  serve  for  wash-water. 

The  investigations  demonstrate  conclu 
sively  that  economy  demands  plain  subsidence 
suplemented  by  a  considerable  period  of 
coagulation  and  subsidence,  followed  at  times 
by  further  application  of  chemicals  to  effect 
coagulation  for  filtration,  in  the  case  that  high 
rates  of  filtration  should  be  employed.  With 
regard  to  the  best  manner  of  carrying  into 
practice  such  an  improvement  there  are  very 
few  specific  data  to  serve  as  a  guide,  as  was 
first  pointed  out  to  you  in  a  general  way  in  a 
preliminary  report  dated  July  11.  1896. 

The  closing  pages  of  Chapter  IV  contain 
the  only  evidence  to  offer  upon  the  subject 
which  was  obtained  in  1896.  Much  additional 
evidence  along  this  line  was  obtained  in  1897, 
and  is  recorded  in  Chapter  XV. 

Provisions  for  Cleaning  the  Settling  Basin  or 
Chamber. — This  matter  was  not  economically 
handled  in  the  case  of  any  of  the  systems. 
Except  in  the  case  of  the  Jewell  it  was  almost 
ignored,  practically  speaking,  and  in  this  sys 
tem  the  provisions  were  inadequate  for 
economical  use. 

Provisions  for  Inspection  of  the  Condition  of 
the  Settling  Basin  or  Chamber. — This  factor 
was  apparently  lost  sight  of  in  all  of  the  svs- 


262 


WATER   PURIFICATION  AT  LOUISVILLE. 


terns,  and  the  failure  to  determine  the  con 
dition  of  the  contents  of  these  compartments 
and  if  necessary  remove  the  accumulation  of 
sludge,  undoubtedly  led  at  times  to  the  pas 
sage  upon  the  filters  of  mud  which  should 
have  been  held  in  the  settling  basins.  The 
effect  of  this  passage  of  mud  on  to  the  filters 
on  the  cost  of  operation  was  to  decrease  the 
length  of  runs  and  therefore  to  increase  the 
percentage  of  water  wasted  and  used  for 
washing.  The  most  notable  occurrence  of 
this  kind  took  place  in  the  Warren  System  on 
July  22  to  27. 

Degree  of  Coagulation  of  the  Water  as  it 
Entered  the  Sand  La\cr. 

One  of  the  most  clearly  established  points 
in  connection  with  these  tests  was  the  abso 
lute  necessity  of  thorough  coagulation  of  the 
water  as  it  entered  the  sand  layer.  With  dif 
ferent  characters  of  water  the  required  de 
gree  of  coagulation  varied  somewhat,  but 
it  was  made  perfectly  clear  that  with  the  high 
rates  of  filtration  employed  in  these  filters  of 
the  American  type  a  high  degree  of  coagula 
tion  is  very  essential. 


In  the  adoption  of  a  system  of  25.000,000 
gallons  capacity,  to  last  for  many  years,  it  is 
very  questionable  whether  wooden  structures 
as  employed  in  the  Warren,  Jewell,  and  West 
ern  Gravity  systems  would  be  advisable  in 
preference  to  metal.  In  all  of  the  systems  it 
would  be  very  desirable  and  probably  prac 
ticable  to  make  the  more  important  parts  of 
the  filters,  such  as  strainer  systems,  more 
readily  accessible.  The  unsatisfactory  results 
from  the  use  of  wood  was  illustrated  by  the 
foul  and  slimy  deposits  upon  the  walls  of  the 
filtered-water  compartment  beneath  the  sand 
layer  of  the  Warren  filter  when  that  system 
was  removed  after  the  close  of  the  tests.  This 
particular  construction  could  and  should  be 
improved. 

Tn  the  filters  of  both  the  Jewell  and  the 
Western  systems,  but  especially  in  the  case  of 
the  latter  filters,  there  was  a  considerable  stick 
ing  together  of  the  sand  grains  at  the  bottom 
of  the  sand  lavers.  This  segregation  of  the 


sand  grains  was  evidently  associated  with  the 
use  of  cement,  and  it  is  possible  that  this 
might  lead  to  serious  difficulty  in  time. 

Sand  Layers  of  the  Several  Filters. 

The  more  important  data  upon  the  several 
sand  layers,  as  they  appeared  at  the  close  of 
the  tests,  are  reported  in  the  foregoing  section 
in  relation  to  the  quality  of  the  effluent.  As 
stated  there,  the  various  data  were  so  compli 
cated  by  a  series  of  factors  that  it  is  impos 
sible  to  draw  conclusions  with  regard  to  sev 
eral  points  of  great  practical  significance. 
The  more  important  points  are  noted  in  turn 
as  follows: 

Thickness. — While  the  Jewell  filter  was 
able  to  yield  the  most  economical  results 
there  is  no  proof  that  it  was  the  best  one 
which  could  be  adopted  with  regard  to  thick 
ness. 

Size  of  Sand  Grain. — In  the  case  of  the 
Jewell  sand  layer  the  most  economical  results 
were  obtained.  But  in  the  case  of  size  of 
grain  as  well  as  thickness  of  layer  there  are  no 
data  to  show  what  would  be  the  most  eco 
nomical  conditions  to  adopt  in  practice.  Tak 
ing  everything  into  consideration,  especially 
the  frequency  of  tiny  flakes  of  aluminum  hy- 
'  drate  in  the  Jewell  effluent,  it  is  probable  that 
a  finer  size  of  grain  would  be  more  advan 
tageous. 

Composition  of  Sand. — It  appears  from  the 
available  evidence  that  as  satisfactory  results 
may  be  obtained  under  suitable  conditions 
from  natural  sand  layers  as  from  those  made 
from  the  more  expensive  crushed  quartz. 


The  location  of  the  sand  layer  in  the  upper 
part  of  the  filter,  with  a  depth  of  three  feet 
or  less  of  water  above  the  sand,  such  as  was 
the  case  in  the  Jewell  and  Western  gravity 
(B)  filters,  is  a  marked  step  in  advance.  By 
the  use  of  a  trap,  and  a  suitable  location  of  the 
point  of  discharge  of  the  effluent,  the  total 
available  head  may  be  undiminished  and  at 
the  same  time  the  following  economical  ad 
vantages  may  be  insured: 

i .  The  difficult  and  in  a  measure  impossi 
ble  task  of  satisfactorily  filtering  all  of  the 


SUMMARY  AND  DISCUSSION   OF  DATA    OF   1895-96. 


26.1 


water  remaining  above  the  sand  just  prior  to 
washing  is  readily  removed  under  normal 
conditions. 

2.  The  quantity  of  chemically  treated 
water,  which  it  is  necessary  to  remove  before 
washing  and  to  either  waste  or  pump  again, 
is  materially  reduced. 

The  second  weakness  \vas  most  noticeable 
in  the  Western  gravity  filter  (A). 

There  is  no  evidence,  however,  to  indicate 
that  the  use  of  a  negative  head  (suction)  has 
any  advantage  other  than  those  stated  above. 

Loss  of  Head. 

Initial. — The  initial  loss  of  'head  is  an  in 
fluential  factor  in  the  cost  of  operation  of  a 
system  of  purification,  in  that  the  available 
head  is  reduced  during  filtration  by  the 
amount  of  the  initial  loss  of  head.  It  is  also 
indirectly  connected  with  the  successful  prac 
tice  of  surface  agitation.  The  initial  loss  of 
head  was  determined  mainly  in  the  case  of 
these  systems  by  the  resistance  of  the  several 
sand  layers.  In  all  cases  the  strainer  systems 
when  clean  offered  apparently  no  measurable 
resistance  to  the  flow  at  the  contract  rate.  In 
the  case  of  the  two  Western  systems,  the  pres 
ence  of  sand  in  the  strainer  tubes  as  above 
noted  probably  increased  the  initial  loss  of 
head  to  a  greater  or  less  degree. 

Maximum. — The  maximum  loss  of  head 
(maximum  acting  head)  which  can  be  utilized 
is  an  important  factor  in  the  cost  of  opera 
tion,  in  that  it  influences  the  length  of  runs 
(period  between  washes)  and  thus  affects  the 
relation  between  the  actual  and  net  rates  of 
filtration. 

In  this  respect  the  respective  filters  be 
haved  very  differently.  The  Warren  and  the 
Western  pressure  filters  were  practically  al 
ways  washed  because  of  the  failure  in  charac 
ter  of  the  effluent  and  not  because  the  resist 
ance  of  the  sand  layers  required  greater 
available  head  than  the  construction  allowed. 
The  reverse  was  true,  except  in  cases  of  pe 
culiar  conditions  of  the  river  water,  with  the 
Jewell  filter.  This  matter  was  discussed  in 
.the  preceding  section  of  this  chapter,  in  re 
gard  to  its  effect  on  the  quality  of  the  efflu 
ent.  A  very  noticeable  point  in  this  connec 
tion  was  mentioned  there,  that  is,  that  during 


Loss 

of  Head  in 

«>et.  j 

Initial. 

Maxii 

num. 

Normal. 

Extreme. 

Jewell  

I   6 

13   6 

65   4 

the  last  of  May  the  composition  of  the  river 
water  was  such  that,  with  the  amounts  of 
chemicals  used,  none  of  the  systems  was  able 
to  obtain  a  degree  of  coagulation  of  the  water 
as  it  entered  the  sand  layer,  sufficient  to  clog 
appreciably  the  layer  before  the  character 
of  the  effluent  failed. 

Almost  without  exception  during  this 
period  the  filters  were  washed  without  any 
appreciable  increase  in  loss  of  head  over  the 
initial. 

A  comparative  idea  of  the  relative  signifi 
cance  of  these  factors  under  the  contract  rate 
of  250,000  gallons  per  twenty-four  hours  is 
indicated  in  the  following  table: 


Pressure  System. 

One  of  the  economical  advantages  claimed 
for  pressure  systems  as  compared  with  grav 
ity  systems  is  that  they  would  lessen  the  cost 
of  purification  by  removing  the  necessity  of 
a  secondary  pumping  of  the  water  if  such 
should  be  the  case  with  gravity  systems.  This 
would  depend  upon  local  conditions,  and 
under  some  circumstances  it  might  be  true. 
But  the  experience  obtained  during  these 
tests  indicates  clearly  that,  with  the  muddy 
Ohio  River  water  at  Louisville,  a  single 
pumping  of  the  river  water  to  and  through 
a  pressure  system  is  out  of  the  question  on  the 
grounds  of  unnecessary  cost.  The  excessive 
cost  attending  the  use  of  a  pressure  system 
would  be  caused  by  the  large  closed  compart 
ments  which  it  would  be  necessary  to  insert 
between  the  main  (primary)  pumps  and  the 
pressure  filters,  in  order  to  secure,  under  the 
existing  conditions,  the  removal  of  mud,  etc., 
which  the  economical  treatment  of  this  water 
before  its  filtration  demands. 

It  may  occur  to  some  that  a  combined  pres 
sure  and  gravity  system  might  be  desirable 
for  the  purification  of  this  water  supply. 
That  is  to  say,  pump  the  water  from  the  river 


264 


WATER   PURIFICATION  AT  LOUISVILLE. 


to  an  elevated  open  subsidence  basin  of  ad 
equate  size,  and  then  allow  the  propeny 
treated  water  to  flow  through  pressure  niters 
on  its  way  from  the  subsidence  basin  to  the 
consumers.  From  the  experience  obtained 
with  the  Western  pressure  filter  the  adoption 
of  this  scheme  would  lead  to  serious  difficul 
ties,  owing  to  irregularities  in  operation  aris 
ing  from  variation  in  the  rate  of  consumption 
at  different  hours  (and  minutes)  of  the  day, 
such  as  the  ordinary  necessities  of  the  con 
sumers  demand. 

Unusual  rates  of  consumption  such  as 
might  occur  in  putting  out  large  fires,  etc., 
would  increase  these  difficulties.  That  irregu 
larities  such  as  would  occur  in  this  way  were 
a  very  serious  matter  in  the  operation  of  the 
Western  System  was  shown  conclusively,  and 
is  so  indicated  by  the  official  communication 
received  from  the  Western  Filter  Company 
on  June  26,  in  explanation  of  the  withdrawal 
from  these  tests  of  their  gravity  system  for  a 
period  of  three  months.  This  letter  was  given 
in  an  earlier  part  of  this  chapter,  in  the  de 
scription  of  Period  No.  18.  In  passing  it  may 
be  mentioned  that  all  experiences  in  water  fil 
tration,  with  which  the  writer  is  familiar, 
point  clearly  to  the  advisability,  if  not  to  the 
necessity,  of  placing  a  reservoir,  not  neces 
sarily  large,  between  the  filters  and  the  dis 
tributing  system  in  order  to  maintain  as  uni 
form  pressure  as  possible  in  the  pipes  and  to 
guard  against  irregularities  in  the  operation 
of  the  filters,  with  their  attending  difficulties. 

Rate  of  Filtration. 

The  rate  of  filtration  is  a  very  prominent 
factor  in  the  cost  of  construction  of  a  large 
system.  It  also  affects  the  cost  of  operation. 
The  available  data  can  only  be  regarded  as 
suggestive  upon  this  point.  The  fact  that  the 
Western  pressure  filter,  however,  yielded  for 
comparatively  long  periods  at  a  time  an  efflu 
ent  which  compared  favorably  with  the 
others  in  character,  at  a  much  higher  rate  per 
unit  of  sand  surface,  is  a  matter  which  cannot 
be  ignored  or  considered  lightly.  This  is 
especially  true  when  it  is  remembered  that  the 
Western  pressure  filter  was  operated  in  the 
face  of  many  complications,  including  irregu 
lar  coagulation,  a  faulty  strainer  system,  and 


Filter. 

Rate  of  Filtration. 

Normal  Clear  Water. 

Muddiest  Water. 

Cubic 
Feet  per 

Minuie. 

Million 
Gallons  per 
Acre  per 
24  Hours. 

Cubic 
Feet  per 

Million 
Gallons  per 
Acre  per 

20.8 
26.3 
23.1 

126 
1  06 
164 

20.1 
22.2 

"3-7 

122 
yo 
97 

Jewell            

Western  Pressure.  . 

absence  of  agitation  of  sand  layer  to  secure 
complete  washing,  etc. 

The  actual  average  rates  of  filtration  em 
ployed  in  the  case  of  the  several  filters  with 
fairly  clear  and  muddiest  water,  respectively, 
are  as  follows: 


The  contract  rate  of  250,000  gallons  per 
twenty-four  hours  is  equivalent  to  23.21  cubic 
feet  per  minute.  Owing  to  different  areas  of 
filtering  surface  this  rate  per  unit  of  area  dif 
fered  for  the  several  filters,  as  follows: 


Filter. 

Area  in  Square  Feet. 

Contract  Rate  in 
Million  Gallons  per 
Acre  per  34  Hours. 

Warren 

141 

Jewell  

94 

Western  Pressure.  . 

66.20 

'57 

That  comparatively  wide  ranges  in  unit 
rates  did  not  affect  the  cost  for  chemicals  by  a 
corresponding  amount  will  be  seen  by  an  in 
spection  of  the  tables  given  in  connection 
with  the  discussion  of  the  effect  of  rate  of  fil 
tration  on  the  quality  of  the  effluent  in  the 
preceding  section.  Some  further  investiga 
tions  along  this  line  were  made  by  the  Water 
Company  during  1897,  and  are  recorded  in 
Chapter  XV. 

Wasliing  the  Sand  Layer. 

The  washing  of  the  sand  layer  was  a  con 
siderable  item  in  the  cost  of  operation  of  the 
respective  systems,  for  two  reasons: 

1.  The  net  rate  of  purification  was  reduced 
as  the  frequency  of  washing  increased,  because 
of  the  increased  percentage  of  water  wasted 
and  used  for  washing. 

2.  The  cost   of  the  operation   of  washing 
was  a  considerable  item,  and  this  was  also  in 
creased   in   total   expense  as  the  number  of 
washes  increased. 

The   chief  factors  affecting  the   frequency 


SUMMARY  AND   DISCUSSION   OF  DATA    OF   1895-96. 


of  washing  have  been  discussed  in  the  pre 
ceding  pages.  It  was  mainly  determined  by 
the  relation  between  the  degree  of  coagula 
tion  of  the  water  as  it  entered  the  sand  layer, 
type  of  sand  layer,  rate  of  filtration,  character 
of  filtered  water,  and  available  acting  head. 
The  relation  of  the  agitation  of  the  surface  of 
the  sand  layer  to  the  frequency  of  washing  is 
discussed  beyond. 

The  cost  of  the  operation  of  washing  was 
dependent  upon  the  amount  of  water  used, 
the  pressure  at  which  it  was  delivered,  and  the 
cost  of  agitation  of  the  sand,  if  employed. 

Amount  of  Water  Used. — The  comparative 
amounts  were  determined  entirely  by  the 
method  of  washing  employed.  In  the  case  of 
the  Warren,  Jewell,  and  Western  Pressure 
systems,  the  average  quantities  for  each  wash 
during  the  entire  investigation  were  528,  627, 
and  633  cubic  feet,  respectively. 

Mctliod  of  ll'its/iing. — All  indications  point 
to  the  conclusion  that  the  most  economical 
method  of  washing  is  to  carry  the  process  to 
a  point  where  all  detachable  materials  are  re 
moved  from  the  sand,  but  no  further.  This 
means  that  it  seems  best  to  wash  the  sand 
until  the  wash-water  after  passage  through  it 
is  practically  clear. 

The  amount  required  depends  principally 
upon  the  amount  and  character  of  the  matter 
accumulated  on  the  sand  grains,  and  upon  the 
relative  efficiency  of  equal  quantities  of  water. 
The  latter  factor  is  dependent  upon  the  dis 
tribution  of  the  water  throughout  the  sand 
layer  and  upon  the  agitation  of  the  sand  layer, 
notably  the  rubbing  together  of  the  sand 
grains  by  the  agitator  teeth. 

During  the  latter  part  of  these  tests  the 
Warren  filter  was  uniformly  washed  to  a  sat 
isfactory  degree.  This  was  the  case  as  a  rule 
in  the  Jc\vell  filter,  but  not  uniformly  so.  The 
Western  pressure  filter  was  almost  never 
washed  as  thoroughly  as  it  should  have  been. 
This  was  probably  the  chief  reason  why  it  was 
necessary  in  this  system  to  waste  the  first  por 
tion  of  the  effluent  after  washing,  owing  to  its 
unsatisfactory  character.  The  amount  wasted 
was  usually  only  a  small  percentage  of  the 
total  water  filtered  on  the  run.  but  during 
muddy  conditions  of  the  river  water  the 
amount  of  filtered  water  wasted  became  pro 


portionately  large  and  at  times  exceeded  in 
amount  the  quantity  of  satisfactory  effluent 
obtained. 

Distribution  of  W'atcr  throughout  the  Sand 
La\er. — The  distribution  of  the  water  during 
washing  was  affected  by  the  agitation  of  the 
sand  layer  and  in  turn  reduced  the  cost  of 
agitation.  The  main  factor  affecting  the  dis 
tribution  was  the  system  used  for  this  pur 
pose. 

The  Warren  distributing  system  was  handi 
capped  for  a  time  during  the  early  part  of  the 
tests  by  having  an  undue  portion  of  the  wash- 
water  deflected  from  the  central  well  through 
a  small  area  of  the  strainer  system  and  sand 
layer.  This  was  apparently'  remedied  to  a 
large  extent  by  the  changes  made  on  Feb 
ruary  12,  1896. 

The  distributing  system  of  the  Jewell  filter 
was  apparently  quite  satisfactory.  The  most 
notable  points  about  this  device  were  the  re 
striction  of  the  neck  of  the  strainer  cups,  and 
the  small  deflector  in  the  cups  just  above  the 
neck.  By  the  first  arrangement  the  greatest 
resistance  to  the  passage  of  the  water  was  met 
at  this  point,  thus  causing  a  distribution  of 
the  water  throughout  the  entire  system.  The 
small  casting  which  was  placed  in  the  cups 
just  above  the  neck  served  to  break  and  de 
flect  the  stream  of  water  just  before  it  entered 
the  sand  layer. 

The  distributing  systems  of  the  Western 
pressure  and  Western  gravity  (A)  filters 
were  handicapped  by  the  presence  of  sand  in 
the  tubes,  as  was  noted  in  the  last  section.  It 
is  difficult  to  determine  how  far  these  dis 
tributing  systems  affected  the  quantity  of 
water  used,  as  these  filters  were  never  washed 
thoroughly. 

In  connection  with  the  distributing  systems 
of  the  Western  filters,  it  is  to  be  noted  that 
when  they  were  clean  there  was  less  restric 
tion  to  the  passage  of  the  water  through  the 
distributing  system  than  in  the  supply  pipe. 
Such  an  arrangement  naturally  involved  the 
passage  of  the  water  most  rapidly  through 
those  portions  of  the  system  nearest  the  con 
nection  with  the  supply  pipe.  The  accumu 
lations  of  sand  in  the  strainer  tubes  reduced 
the  total  outlet  area  and  therefore  increased 
the  resistance  of  the  tubes.  These  accumula- 


266 


WATER   PURIFICATION  AT  LOUISVILLE. 


tions,  furthermore,  increased  the  tendency  of 
the  water  to  pass  into  comparatively  small 
portions  of  the  sand  layer. 

The  ball-nozzle  system  of  the  Western 
gravity  filter  (E)  \vas  not  in  use  for  a  suf 
ficient  length  of  time  to  determine  its  relative 
efficiency.  Observations  during  and  after 
construction,  however,  indicated  unequal  dis 
tribution  of  the  water  at  different  parts  of  the 
sand  layer. 

The  mechanical  agitation  of  the  sand  layer 
during  washing  greatly  aided  in  distributing 
the  wash-water  and  increased  the  relative 
efficiency  of  equal  quantities  of  water.  The 
Jewell  and  Warren  systems  used  mechanical 
devices  for  agitating  the  sand  throughout  the 
tests.  The  current  of  water  was  relied  upon 
for  agitation  in  both  the  Western  filters.  In 
this  connection  it  is  to  be  noted  that  a  modi 
fication  in  the  mechanical  agitators  whereby 
the  sand  would  be  floated  to  a  less  degree 
and  the  grains  rubbed  together  more  than 
was  the  practice  in  these  tests  suggests  an 
economical  advance,  as  equally  satisfactory- 
results  might  be  obtained  with  the  use  of  less 
wash-water. 

Pressure  of  Wash-mater. — The  pressure 
under  which  the  water  was  delivered  at  the 
inlet  of  the  distributing  systems  is  the  second 
factor  in  the  cost  of  the  operation  of  washing. 
This  was  widely  different  in  the  case  of  the 
several  filters  at  times  during  the  tests,  on 
account  of  changes  in  other  factors.  The  ef 
ficiency  of  the  various  .  pressures  used  de 
pended  largely  upon  the  amount  and  dis 
tribution  of  the  resistances  of  the  distributing 
systems.  The  increased  resistance  of  the  dis 
tributing  systems  of  the  Western  filters,  due 
to  the  presence  of  sand  in  the  tubes,  was 
clearly  shown  by  the  increases  made  from 
time  to  time  in  the  pressure  employed.  The 
use  of  mechanical  agitators  greatly  decreased 
-the  pressure  required,  as  was  shown  by  the  in 
crease  in  pressure  used  by  the  Jewell  filter, 
as  the  efficiency  of  the  agitator  decreased. 
Owing  to  these  and  other  factors  it  is  difficult 
to  estimate  the  pressure  necessarv  under  nor 
mal  conditions  of  operation.  The  following 
table  gives  the  pressures  which  were  used  at 
the  close  of  the  tests,  in  pounds,  of  the  water 
at  the  inlet  to  the  several  distributing  sys 
tems: 


2.O 

7-5 
5-9 


Agitation  of  the  Sand  Layer. — in  the  West 
ern  pressure  filter  the  sand  layer  was  never 
agitated  except  by  the  current  of  wash-water 
— unless  the  removal  of  sand  to  repair  the 
strainer  system  be  so  regarded.  Agitation 
was  regularly  employed  in  the  Warren  and 
Jewell  sand  layers.  All  indications  point  to 
a  decided  advantage  in  the  constant  agitation 
during  washing. 

The  Warren  agitator  was  changed  and  re 
paired  several  times,  and  during  the  later  part 
of  the  tests  appeared  to  fulfill  its  purpose. 
Considerable  difficulty  was  experienced  with 
the  Jewell  agitator  on  acount  of  its  stopping 
and  refusing  to  work  at  frequent  intervals. 
At  first  this  was  thought  to  be  due  to  the  use 
of  too  small  an  engine  (nominally  5  H.P.)  or, 
perhaps,  to  some  obstructions  of  the  strainer 
system.  Careful  inspection,  however,  led  to 
the  conclusion  that  it  was  caused  by  a  binding 
of  the  gears,  due  to' a  warping  yf  the  timbers 
upon  which  the  agitator  rested.  This  could 
be  readily  remedied  by  a  more  careful  con 
struction.  The  devices  for  agitation  could  and 
should  be  improved  in  simplicity  of  construc 
tion,  and  in  both  the  Warren  and  Jewell  sys 
tems  the  devices  were  too  weak  for  their  pur 
pose.  As  noted  above,  an  improvement  in 
these  devices  whereby  the  sand  grains  would 
be  rubbed  together  more  energetically  would 
probably  result  in  a  saving  of  wash-water. 

Pou<cr  Used  for  Agitation. — At  the  close  of 
the  tests,  with  the  pressure  and  quantities  of 
wash-water  then  in  use,  the  power  required  to 
operate  the  agitators  of  the  Warren  and 
Jewell  systems  was  as  follows: 


Warrer 
Jewell. 


The  maximum  power  required  occurred  in 
the  Warren  at  the  time  of  lifting  the  rakes 
and  in  the  Jewell  at  the  time  of  forcing  the 
rakes  into  the  sand  and  starting  them  in  mo 
tion. 


SUMMARY  AND   DISCUSSION  OF  DATA    Ol<    1895-96. 


267 


Surface  Agitation. 

In  the  case  of  the  Jewell  System  it  was 
found  that  with  certain  conditions  of  river 
water,  and  of  its  coagulation,  the  resisting 
layer  of  mud  on  the  surface  of  the  sand  could 
he  broken  up  and  filtration  then  continued 
without  washing  the  filter  or  injuring  the 
character  of  the  effluent.  This  operation, 
when  successful,  reduced  the  resistance  of  the 
sand  layer  and  so  lengthened  the  run.  It  was 
therefore  an  element  of  more  or  less  magni 
tude  in  the  consideration  of  cost,  in  that  it 
decreased  the  frequency  of  washing.  The 
success  of  surface  agitation  was  very  closely 
dependent  on  the  degree  of  coagulation 
of  the  water  as  it  entered  the  sand  layer, 
and  on  the  character  of  the  sand.  In  these 
tests  the  use  of  surface  agitation  at  times  of 
very  muddy  water,  or  when  the  river  water 
contained  large  amounts  of  fine  clay,  was  not 
as  a  rule  attempted,  and  when  tried  was  not 
successful.  The  cause  of  the  failure  seems 
clearly  to  have  been  the  incomplete  coagula 
tion  of  the  water  at  these  times. 

Relation  of  Proper  Attention  and  Supervision  to 

the  Econoin\  of  Purification  of  the  Ohio 

River  Water  by  this  Method. 

This  subject  has  been  referred  to  in  Chap 
ter  VII,  and  again  in  this  chapter  in  relation 
to  the  efficiency  of  filtration.  The  most 
marked  effect  of  proper  supervision  of  the  op 
eration  of  these  systems  was  on  the  cost  of 
treatment.  As  has  already  been  presented, 
there  is  at  all  times  a  certain  optimum  amount 
of  chemical,  below  which  satisfactory  results 
cannot  be  obtained,  and  above  which  all 
chemical  used  is  practically  wasted.  In  the 
light  of  our  present  knowledge  the  deter 
mination  of  this  optimum  amount,  for  such  a 
rapidly  and  widely  varying  character  of  water 
as  that  of  the  Ohio  River,  is  a  very  difficult 
problem.  At  times  the  optimum  amount 
could  be  very  clearly  determined  by  one  thor 
oughly  familiar  with  the  methods  of  proced 
ure,  while  at  other  times,  especially  with 
water  which  would  give  a  clear  effluent  con 
taining  large  numbers  of  bacteria,  the  de 
cision  required  judgment  based  on  extended 
experience. 


A  system  of  purification  of  the  Ohio  River 
water  is  clearly  one  of  combinations  of 
methods  and  devices,  which  experience  has 
demonstrated  cannot  be  handled  economi 
cally  by  unskilled  labor.  It  would  be  easv  for 
untrained  attendants  to  waste  many  thou 
sands  of  dollars  annually  by  the  needless  use  of 
the  chemical.  A  comparison  of  the  average 
daily  cost  of  the  chemical  used  during  each 
of  the  periods  by  the  Warren,  Jewell,  and 
Western  pressure  systems,  on  a  net  basis  of 
25  million  gallons  daily,  is  represented  in  the 
following  table  and  shows  this  point. 


DAILY   COST    FOR    CHEMICAL. 


Period. 

Warren  System. 

Jewell  System. 

Western  Pressure 
System. 

I 

V 

$37.00 

2 

67  .  oo 

49  .00 

3 

22g.OO 

134.00 

f  1  5  2  .  oo 

4 

231  .OO 

52.00 

57.00 

c. 

26  1  .  OO 

225.00 

1  20.00 

6 

252.CO 

1  29  .  oo 

201  .00 

7 

226.OO 

1  5  5  .  oo 

134.00 

8 

208.00 

60.00 

46.00 

9 

423  oo 

264.00 

239.00 

0 

280.00 

I  99  .  oo 

204.00 

I 

324.00 

76  .co 

269.00 
76  .00 

224.00 

3 

80.00 

96.00 

59.00 

4 

76.00 

69.00 

64.00 

5 

295.00 

300.00 

395.00 

6 

235.00 

300  .  oo 

288.00 

7 

152.00 

267.00 

275.00 

8 

2Q7.OO 

437-0° 

548.00 

9 

1  79  .  oo 

354.00 

335.00 

20 

416.00 

575-oo 

536.00 

In  less  skilled  hands  these  variations  would 
probably  have  been  more  marked.  With  an 
adequate  employment  to  its  economical  limits 
of  subsidence  both  with  and  without  coagu 
lation,  the  necessity  for  variation  in  the 
amount  of  applied  chemical  would  be  much 
less,  and  the  opportunity  for  departure  from 
the  optimum  amount  would  be  reduced 
materially.  Nevertheless,  there  would  be  no 
condition  where  this  river  water  could  be 
economically  purified  except  by  skilled  labor 
and  supervision. 

Jt  is  true  that  the  above  data  are  compli 
cated  by  other  factors,  some  of  which  vary 
from  time  to  time,  but  they  serve  to  illustrate 
the  point  in  question  to  a  very  considerable 
degree. 


WATER   PURIFICATION    AT   LOUISVILLE. 


SECTION  No.  4. 

COMPARISON  OF  THE  ELEMENTS  OF  COST  OF 
PURIFICATION  OF  TWENTY-FIVE  MIL 
LION  GALLONS  OF  OHIO  RIVER  WATER 
DAILY  BY  THE  RESPECTIVE  SYSTEMS, 
BASED  ON  THE  RESULTS  OF  THESE  IN 
VESTIGATIONS. 

in  the  following  pages  are  given  the  ele 
ments  of  probable  cost,  so  far  as  it  is  feasible, 
of  the  purification  of  25  million  gallons  of 
Ohio  River  water  daily  by  each  of  the  sys 
tems  representing  the  method  in  which  co 
agulation  and  partial  sedimentation  by  alu 
minum  hydrate  formed  from  sulphate  of 
alumina,  and  subsequent  rapid  filtration,  were 
employed.  As  a  matter  of  convenience  the 
elements  of  cost  are  subdivided  into  those  of 
construction  and  those  of  operation.  All  of 
these  estimates  are  based  on  the  results  ob 
tained  from  these  investigations,  upon  the  op 
eration  of  small  test  systems  contracted  to 
purify  250,000  gallons  per  twenty-four  hours. 
From  the  nature  of  the  existing  conditions 
at  this  time,  and  in  the  absence  of  definite 
knowledge  as  to  the  cost  of  the  various  de 
vices,  these  estimates  of  necessity  deal  for  the 
most  part  with  elements  of  cost.  They  are 
so  arranged  that  when  the  exact  cost  of  the 
several  devices  is  known,  the  aggregate  cost 
may  be  readily  computed.  Wherever  the  ex 
isting  conditions  permit  of  it,  actual  estimates 
of  cost  are  given. 

The  following  data  are  summaries  of  the 
principal  elements  of  cost  of  the  respective 
svstems  as  demonstrated  in  the  previously  de 
scribed  investigations.  In  so  far  as  possible 
the  several  amounts  have  been  determined 
and  estimated  on  the  basis  of  a  normal  or 
slightly  muddy  river  water  containing  about 
100  parts  per  million  of  suspended  matter,  and 
also  for  a  fairly  muddy  river  water  containing 
about  1800  parts.  The  majority  of  the  com 
parisons  call  for  normal  and  maximum  fig 
ures,  but  in  some  cases  representative  aver 
ages  for  these  tests  are  required.  In  the  latter 
instance  the  data  presented  in  Table  No.  5 
are  used.  Under  the  conditions  of  proper 
preliminary  treatment  before  filtration  by  sub 
sidence  with  and  without  the  aid  of  coagu 


lants,  it  might  be  expected  that  the  water 
which  reached  the  niters  would  compare  with 
the  normal  river  water  as  used  in  these  sum 
maries.  On  the  other  hand,  the  figures  given 
for  the  muddiest  water  do  not  represent  the 
extremes  which  would  be  obtained  under  con 
ditions  of  actual  muddiest  water  in  the  Ohio 
River.  Such  conditions  are.  however,  un 
usual  and  of  comparatively  short  duration, 
and  for  these  data  reference  is  made  to  the 
tables  of  individual  runs  which  were  pre 
sented  in  Chapter  Yll  I.  As  a  rule  the  figures 
given  as  maximum  in  the  following  sum 
maries  are  averages  for  Period  No.  20,  ex 
cluding  those  runs  which  were  affected  by  the 
period  of  subsidence  over  night,  or  were 
otherwise  abnormal.  It  will  be  seen  by  refer 
ence  to  Chapter  VIII  that  on  July  24,  1896, 
the  amount  of  suspended  matter  in  the  river 
water  was  3347  parts  per  million,  or  nearly 
double  the  amount  which  is  considered  as  the 
average  muddiest  water.  (The  maximum 
amount  of  suspended  solids  found  during  the 
entire  investigations  was  5311  parts  per  mil 
lion  on  March  6,  1897.) 

These  excessively  high  amounts  would 
probably  never  reach  the  filter  in  practice, 
where  proper  provision  for  preliminary  plain 
subsidence  was  made;  and,  with  the  use  of 
coagulation  and  subsidence  as  mentioned 
above,  the  water  reaching  the  filters  would 
probably  not  be  excessively  muddy. 

The  Western  gravity  filter  (A)  does  not 
appear  in  these  comparisons  because  it  was 
found  to  be  unable  to  purify  at  all  times 
enough  water  to  wash  its  own  sand  layer,  and 
its  operation  was  discontinued  by  the  West 
ern  Filter  Company. 

The  Western  gravity  filter  (B)  was  not 
operated  long  enough  to  yield  adequate  data, 
but  there  are  no  indications  of  its  being  com 
parable  to  the  Warren  or  Jewell  filters.  As 
will  be  seen  on  examinations  of  the  tables  in 
Chapter  VI 1 1,  the  percentage  which  the  wash 
and  waste  water  was  of  the  applied,  exceeded 
100,  three  times  in  the  case  of  the  Western 
pressure  filter  and  once  in  the  case  of  the 
Jewell  filter.  As  the  contiguous  results  indi 
cate  that  these  percentages  were  abnormal, 
they  have  not  been  considered  as  liable  to 
i  occur  in  regular  practice. 


SUMMARY  AND   DISCUSSION  OF  DATA    OF   1895-96. 
Summaries  of  Elements  of  Cost. 


269 


NOKMAI.  PERIOD  OK  SKKYICK  OK  THE  FILTERS  OK  THE 
RESPECTIVE  SYSTKMS  BETWEEN  WASIIKS.  HOURS  AND 
MI.NUTHS.  • 

System.  Ordinary  Water.       Muddiest  Water. 

Warren ioh.  48111.  2h.  oSm. 

Jewell ifih.  38111.  2h.  17111. 

Western  Pressure 1311,38111.  ill.  3801. 

NORMAL  PERIOD  REQUIRED  KOR  WASHING  THE  SAND 
LAYERS  OK  THE  RESPECTIVE  SYSTEMS.     MINUTES. 

System.  Average. 

Warren 26m. 


NORMAL  PERIOD  USKD  FOR  WASTING  UNSATISFACTORY 
FILTERED  WATER  AFTER  WASHING  THE  SAND  LAYERS 
OK  THK.  RESPECTIVE  SYSTEMS.  MINIFIES. 

System.  Ordinary  Water.      Muddiest  Water. 

Warren o  o 

Jewell o  o 

Western  Pressure 14 

NORMAL  QUANTITY  OK  RIVER  WATER  APPLIED  TO  THE 
RESPECTIVE  SYSTEMS,  IN  GALLONS  PER  24  HOURS. 

System.  Ordinary  Water.  Muddiest  Water. 

Warren ....    206  ooo  182  oco 

Jewell      271000  213000 

Western  Pressure      248500  152000 

NORMAL  QUANTITY  OF  COAGULATED  AND  PARTIALLY 
CLARIFIED  WATER  WASTED  BY  THE  RESPECTIVE  SYSTEMS 
PRIOR  TO  WASHING  THE  SAND  LAYERS,  IN  GALLONS 
PER  24  HOURS. 

System.  Ordinary  Water.  Muddiest  Water. 

Warren 960  14  ooo 

Jewell    o  4  ono 

Western  Pressure o  o 

NORMAL  QUANTITY  OK  FILTERED  WATER  USED  IN  WASHING 
THE  SAND  LAYERS  OF  THE  RESPECTIVE  SYSTEMS,  IN  GAL 
LONS  PER  24  HOURS. 

System.  Ordinary  Water.  Muddiest  Water. 

Warren    ...    10  800  47  200 

Jewell          6  2oo  49  200 

Western  Pressure.  ...    8  500  71  700 

NORMAL  QUANTITY  OK  FILTERED  WAFER  WASTED  BY  THE 
RESPECTIVE  SYSTEMS.  OWING  TO  UNSATISFACTORY  AP 
PEARANCE,  IN  GALLONS  PER  24  HOURS. 

System.  Ordinary  Water.  Muddiest  Water. 

Warren    o  o 

Jewell    o  300 

Western  Pressure 2  200  16  300 

NORMAL  NET  QUANTITY  OK  FILTERED  WATER  (EXCLUSIVE 
OK  WASH  WATER  AND  WASTE  WATER)  YIELDED  HY  THE 
RESPECTIVE  SYSTEMS,  IN  GALLONS  PER  24  HOURS. 

System.  Ordinary  Water.      Muddiest  Water. 

Warren 200  ooo  1 20  ooo 

Jewell 266  ooo  if)O  ooo 

Western  Pressure 238  ooo  64  ooo 

NORMAL  NET  QUANTITY  OF  FILTERED  WATER  (EXCLUSIVE 
OF  WASH  WATER  AND  WASTE  WATER)  YIELDED  BY  THE 
RESPECTIVE  SYSTEMS,  IN  MILIION  GALLONS  PER  24 
HOURS  PER  ACRE  OK  FILTERING  SURFACE. 


NORMAL  PERCENTAGE  WHICH  THE  SUM  OK  THE  WASH 
WATER  AND  WASTE  WATER  FORMED  OK  THE  RIVER 
WATER  APPLIED  TO  THE  RESPECTIVE  SYSTEMS. 

System.  Ordinary  Water.  Muddiest  Water. 

Warren 6  34 

Jewell 2  25 

Western  Pressure 4  58 

NORMAL  RATE  AND  PRESSURE  AT  WHICH  THE  FILTERED 
WATER  WAS  SUPPLIED  FOR  WASHING  THE  SAND  LAYERS 
OF  THE  RESPECTIVE  SYSTEMS. 

if  -,,..  ;.,  r.,11^,^         Pressure  in  Pounds  per 

System.  ncrMinuu  Square  Inch  at  the   Bottom 

of  the  Sand  Layer. 

Warren 460  2 .  o 

Jewell 530  7.5 

Western  Pressure 650  5.9 

NORMAL  QUANTITY  OF  APPLIED  SULPHATE  OK  ALUMINA 
IN  GRAINS  PER  GALLON  OF  RIVER  WATER  SUPPLIED  TO 
THE  RESPECTIVE  SYSTEMS. 

System.  Ordinary  Water.  Muddiest  Water. 

Warren 1.41  6.77 

Jewell 1.76  8.74 

Western  Pressure   1 .06  5-27 

NORMAL  QUANTITY  OK  APPLIED  SULPHATE  OF  ALUMINA 
IN  GRAINS  PER  GALLON  OF  NET  FILTERED  WATER 
YIELDED  BY  THE  RESPECTIVE  SYSTEMS. 


JO. 20  3.00 

10.86  2.65 

I  2 . 60  2.72 


System. 

Warien 

Jewell 

Western  Pressure 


Using  the  foregoing  data  as  a  basis  of  com 
putation,  the  following  principal  elements  of 
cost  of  installation  and  operation  of  a  system 
of  25  million  gallons  daily  capacity  are  pre 
sented,  with  actual  estimates  of  cost  wherever 
it  is  feasible. 

NUMBER  OF  THE  RESPECTIVE  UNIT  SYSTEMS  WHICH  WOULD 
BE  NECESSARY  TO  FURNISH  25  MILLION  GALLONS  DAILY 
OF  PURIFIED  WATER  AT  TIMES  OF  ORDINARY  RIVER 
WATER. 

Warren  System   1 24 

Jewell  System 94 

Western  Pressure  System 105 

NUMBER  OF  THE  RESPECTIVE  UNIT  SYSTEMS  WHICH  IT- 
WOULD  BE  NECESSARY  TO  HOLD  is  RESERVE  IN  ORDER 
TO  SUPPLY  25  MILLION  GALLONS  DAILY  OK  PURIFIED 
WATER  AT  TIMES  OF  MUDDIEST  RIVER  WATER. 

Warren  System 85 

Jewell  System 62 

Western  Pressure  System   287 

TOTAL  NUMBER  OF  THE  RESPECTIVE  UNIT  SYSTEMS  WHICH 
WOULD  BE  REQUIRED  TO  SUPPLY  UNIFORMLY  25  MILLION- 
GALLONS  DAILY  OF  PURIFIED  OHIO  RIVER  WATER. 

Warren  System 208 

Jewell  System' 156 

Western  Pressure  System 391 

RATE  IN  CUBIC-  FEET  PER  MINUTE  AT  WHICH  THE  WASH 
WATER  WOULD  HAVE  TO  BE  SUPPLIED  TO  WASH  THE 
SAND  LAYERS  OK  A  25  MILLION  GALLON  PLANT. 

Warren  System 2650  312 

Jewell  System. 1775  177 

Western  Pressure  System 8  560  219 


WATER    PURIFICATION   AT  LOUISVILLE. 


The  head  against  which  the  pump  would 
have  to  operate  in  furnishing  the  wash-water 
would  depend  largely  upon  the  relative  loca 
tion  of  the  pump  and  the  different  niters  with 
reference  to  the  source  of  supply,  but  it  would 
be  such  that  the  available  pressure  on  the 
bottom  of  the  sand  layer  would  be  about  5, 
JO,  and  8  pounds  for  the  Warren,  Jewell,  and 
Western  Pressure  systems,  respectively. 

There  would  be  required,  in  the  case  of  the 
Warren  and  Jewell  systems,  engines  to  fur 
nish  the  power  necessary  to  operate  the  agi 
tating  machinery  when  the  sand  layers  were 
being  washed.  On  the  basis  of  the  above 
data,  the  maximum  and  average  amounts  of 
power  required  for  this  purpose  would  be  as 
follows: 

Maximum.       Average. 

Warren  System    383  H.P      45  H.  P. 

Jewell  System 2So      "         25 

In  addition  to  the  above  elements  of  cost  of 
installation  of  a  25  million-gallon  plant  there 
would  be  the  cost  of  suitable  preparation  of 
the  grounds  upon  which  to  locate  the  system, 
and  also  the  buildings  to  house  the  niters. 

The  area  occupied  by  the  total  number  of 
required  unit  systems  on  the  above  basis 
would  be  as  follows: 


With  regard  to  the  cost  of  application  of 
the  sulphate  of  alumina,  the  very  small  amount 
of  power  required  depends  largely  upon  the 
location  and  arrangement  of  the  system, 
strength  of  solution  used,  etc.,  in  the  case  of 
all  of  the  systems. 

Another  important  factor  connected  with 
the  cost  of  operation  of  such  a  system  of  puri 
fication,  and  also  with  the  installation,  is  the 
extra  pumping  of  the  supply  of  water.  To  a 
great  extent  this  factor  is  dependent  upon 
other  details  of  construction  and  would  prob 
ably  exceed  somewhat  the  minimum.  A  very 
close  idea  can  be  obtained  of  the  importance 
and  significance  of  this  factor  by  considering 
simply  the  difference  in  level  of  the  water 
above  and  below  the  sand  layers  of  the 
several  filters  (loss  of  head).  Taking  these 
figures  as  presented  in  foregoing  tables,  4.5, 
13.6,  and  65.4  feet  for  the  Warren,  Jewell, 
and  Western  Pressure  systems,  respectively, 
and  adding  to  the  total  net  capacity  of 


25  million  gallons  daily  the  average  percent 
ages  of  water  wasted  and  used  for  washing  the 
sand  layers,  6,  2,  and  4  per  cent,  for  ordinary 
water,  and  34,  25,  and  58  per  cent,  for  mud 
diest  water  for  the  three  systems  in  the  order 
above  given,  the  following  amounts  of  power 
required  are  obtained: 


In  regard  to  the  Western  Pressure  System 
it  is  only  fair  to  state  that  with  the  normal 
maximum  loss  of  head  of  20  feet  these  figures 
would  be  reduced  to  about  30  per  cent,  of  the 
figures  given.  The  question  of  the  insertion 
of  pressure  filters  in  the  direct  line  of  pipe 
from  the  main  pumps  to  the  reservoir  or  from 
the  reservoir  to  the  city  has  already  been 
shown  to  be  out  of  the  question;  and  it  is 
only  necessary  to  add  that  the  cost  of  in 
creased  pumping  is  represented  by  the  above 
figures  no  matter  where  the  filters  are  located. 

The  principal  cost  of  operation  would  be 
that  of  the  sulphate  of  alumina  required  for 
coagulation  of  the  river  water.  Using  the 
present  quotations  of  1.5  cents  per  pound  for 
commercial  sulphate  of  alumina  delivered  in 
carload  lots  free  on  board  cars  at  Louisville, 
the  estimates  of  cost  based  on  the  above  data 
are  as  follows: 

DAILY  COST  OF  SULPHATE  OF  ALUMINA  IN  THE  PURIFICA 
TION  OF  25  MILLION  GALLONS  OF  OHIO  RIVF.R  WATER 
BY  THE  RESPECTIVE  SYSTEMS. 


Warren  System 

Jewel]  System 

Western  Pressure  Svsteni 


§547 
584 
676 


142 
146 


FICATION  OF  2^  MILLION-  GALLONS  OF  OHIO  RIVER  WATER 


DAILY    HY   THE    RESPECI  m<:    SYSTEMS,    RASED   ON    THE 


QUANTITY  OF  WATER  IN  GALLONS  PER  DAY,  WHICH  WOULD 
BE  WASTED  AND  USED  FOR  WASHING  THE  SAND  LAYERS 
OF  THE  RESPECTIVE  SYSTEMS  IN  THE  PURIFICATION  OF 
25  MILLION  GALLONS  DAILY  OF  THE  OHIO  RIVER  WATER. 


Wa 


Experience  during  these  tests  showed 
clearly  enough  that  to  purify  25  million 
gallons  of  the  Ohio  River  water  daily  in 


SUMMARY  AND   DISCUSSION   OF  DATA    OF   1895-96. 


271 


all  its  varying  stages  and  conditions, -without 
wasting  sulphate  of  alumina  and  at  the  same 
time  giving  a  purified  water  of  a  satisfactory 
character,  was  absolutely  out  of  the  question 
in  the  absence  of  constant  care  and  skillful 
supervision.  The  attention  given  to  each  sys 
tem  of  a  rated  capacity  of  250,000  gallons  per 
twenty-four  hours  was  of  course  several  times 
greater  than  would  be  necessary  in  a  portion 
of  corresponding  si/e  in  a  system  having  a 
capacity  of  25  million  gallons  daily.  The 
amount  and  scope  of  necessary  analytical 
work  would  also  be  much  modified  in  actual 
practice,  especially  after  a  large  system  had 
been  in  operation  for  a  sufficient  period  for 
the  formulation  of  a  practical  and  systematic 
method  of  procedure. 

The  best  idea  which  can  be  given  you  at 
this  time  as  to  the  cost  of  the  necessary  atten 
tion  for  the  operation  of  a  system  to  purify 
25  million  gallons  of  the  Ohio  River 
water  daily  is  afforded  by  the  statement  that 
it  would  certainly  not  be  less  than  that  for  the 
proper  operation  and  maintenance  of  your 
present  pumping  station,  which  I  understand 
is  14,000  dollars  per  annum. 

SECTION  No.  5. 
GKNKRAL  CONCLUSIONS. 

The  practical  results  of  these  tests,  as  ap 
plied  to  the  problem  of  purifying  the  Ohio 
River  water  for  the  supply  for  the  city  of 
Louisville  may  be  summed  up  in  the  follow 
ing  manner,  in  which  reference  is  made  to  the 
general  applicability  of  the  method  investi 
gated  and  to  the  relative  merits  and  demerits 
of  the  respective  systems. 

Applicability  of  the  Method  to  the  Clarification 
and  Purification  of  the  Ohio  River  Water. 

These  tests  and  investigations  have  proved 
conclusively  that  the  general  method  em 
bodying  subsidence,  coagulation  and  filtra 
tion  is  most  suitable  for  the  proper  and 
economical  purification  of  the  Ohio  River 
water  at  this  city.  With  regard  to  the  use  of 
coagulants  it  may  be  stated  in  unqualified 
terms  that  their  use  is  imperative  for  this 
water,  because  for  at  least  six  to  ten  weeks  in 
the  spring  and  early  summer  the  Ohio  River 
water  contains  such  large  quantities  of  fine 


clay  particles,  many  of  which  are  smaller  than 
bacteria,  that  clarification  and  purification 
without  coagulation  would  be  impracticable  if 
not  impossible. 

While  this  general  method,  which  was  fun 
damentally  adopted  by  each  of  these  systems, 
is  the  most  suitable  one,  in  the  light  of  our 
present  knowledge  concerning  the  science 
and  art  of  water  purification,  yet  in  no  case 
did  the  systems  tested  carry  out  these  prin 
ciples  in  a  manner  demanded  by  the  economi 
cal  and  efficient  purification  of  this  water. 
Expressed  in  briefest  terms,  the  reason  of  this 
was  that  they  failed  to  remove  the  suspended 
matter  sufficiently  before  the  water  reached 
the  sand  layer.  With  regard  to  the  relative 
advantages  of  American  and  English  filters 
for  the  purification  of  the  water,  after  its  par 
tial  clarification  bv  subsidence,  aided  at  times 
by  coagulation,  no  data  were  obtained  at  this 
time,  although  in  Chapter  XVI  the  question 
is  referred  to  briefly  in  reference  to  an  earlier 
series  of  tests  with  English  filters,  made  by 
this  Company. 

The  genera!  defects,  with  their  practical 
significance,  will  next  be  pointed  out  by  a  full 
comparative  summary  of  the  principal  fea 
tures  and  devices  of  the  several  systems.  After 
this  is  presented  in  brief  the  quality  of  the  fil 
tered  water;  and,  at  the  end,  the  final  con 
clusion  from  this  portion  of  the  investigation. 

General  Defect  of  all  Systems,  i^'itJi  its  Results 
in  the  Application  of  this  Method  of  Purifi 
cation  to  the  Ohio  River  Water. 

In  this  connection  it  is  to  be  clearly  borne 
in  mind  that  the  Ohio  River  water  possesses 
a  marked  variability,  both  as  to  character  and 
amount  of  suspended  matter  contained  in  it, 
and  at  times  the  amounts  are  extraordinarily 
large.  This  water,  it  may  be  fairly  said,  is  a 
much  more  difficult  one  to  purify  than  those 
waters  concerning  which  data  upon  purifica 
tion  are  available,  and  which  have  been 
treated  on  a  large  scale  by  American  filters. 
In  justice  to  the  several  filter  companies  it  is 
to  be  stated  that  they  entered  these  tests  with 
systems  which  represented  their  best  devices 
based  upon  their  general  information  and  ex 
perience  when  arrangements  were  made  for 
these  tests,  and  not  with  devices  designed  to 
meet  the  specific  requirements  of  this  case. 


272 


WATER   PURIFICATION  AT  LOUISVILLE. 


Of  the  defects  possessed  by  the  systems  in 
these  tests  there  is  one  which  causes  all  others 
to  drop  into  almost  complete  insignificance. 
As  stated  above,  this  great  defect  was  the  fail 
ure  to  remove  suspended  matter  sufficiently 
from  the  water  as  it  reached  the  sand  layer 
of  the  filter,  in  each  case.  This  would  pro 
duce  the  following  effects  upon  the  process: 

1.  It  would  increase  to  an  excessive  degree 
the  cost  of  a  chemical  to  serve  as  a  coagulant, 
which  is  the  principal  item  of  expense  in  this 
method  of  purification  of  this  water. 

2.  It  would  necessitate  a  reserve  portion  of 
the    system    with    all    the    appurtenances    to 
handle  the  water  when  in  its  muddiest  con 
dition.     In  the  best  systems  this  reserve  por 
tion  would  have  to  be  from  no  to  80  per  cent, 
of  the  system  regularly  in  use. 

3.  It  would  necessitate  at  times  of  muddy 
water  the  waste  of  an  unusually  large  amount 
of  filtered  water  for  the  purpose  of  washing 
the  sand  layers.     When  the  river  water  is  in 
its  muddiest  condition  this  percentage  in  the 
case  of  the  best  system  would  average  from 
25  to  35  per  cent.,  and  might  for  short  inter 
vals  reach  nearly  double  the  average. 

4.  It   would   necessitate,   by   virtue   of  the 
water  thus  disposed  of,  an  increase  in  the  nor 
mal  pumping  appliances,  and,  therefore,  the 
aggregate  cost  of  pumping. 

5.  Owing  to  the  wide  variations  in  the  char 
acter  of  the  water  as  it  reached  the  sand  layer, 
it  would  make  very  difficult  the  task  of  oper 
ating   the   systems  so   as   to   secure   efficient 
purification  at  the  least  possible  cost. 

6.  It  would  necessitate  regularly  a  large  set 
of  trained  attendants  to  operate  the  reserve 
portion  of  the  system,  beside  those  regularly 
engaged  in  operating  the  portion  of  the  sys 
tem  regularly  employed. 

7.  It    would    increase    certain    undesirable 
features  of  the  filtered  water  with  reference 
to  its  corroding  and  incrusting  powers. 

This  defect  was  so  great  in  the  case  of  the 
W'estern  gravity  filter  (A)  that  when  the 
river  was  very  muddy  it  was  unable  to  yield 
enough  filtered  water  to  wash  its  own  sand 
layer,  as  already  stated.  For  this  reason 
this  filter  will  not  be  mentioned  further. 
With  regard  to  the  Western  gravity  filter 
(B),  it  was  not  operated  long  enough  to  al 
low  adequate  data  to  be  secured,  but  gave 


no  indications  of  being  comparable  to  the 
Warren  or  Jewell  filters.  It  will  not  be  men 
tioned  again  in  this  connection. 

The  systems  were  not  perfect  in  other  re 
spects,  but  none  of  the  remaining  weaknesses 
were  of  such  vital  importance  as  was  the  one 
above. 


Herewith  is  presented  a  comparison  of  cor 
responding  devices  of  the  respective  systems 
with  regard  to  their  applicability  in  treating 
the  Ohio  River  water  successfully  by  the 
method  of  purification  under  consideration. 

ritiin  Subsidence. — All  of  the  systems  were 
totally  lacking  in  this  very  essential  requisite 
for  the  most  economical  and  efficient  clarifi 
cation  and  purification  of  this  water. 

Kind  of  Chemical  Used. — Sulphate  of  alu 
mina  was  the  principal  coagulating  chemical 
used  in  these  tests.  So  far  as  could  be  learned 
at  this  time  its  use  was  satisfactory  for  the  re 
quired  purpose. 

Potash  alum  was  used  in  the  Western  Sys 
tems  only  because  of  its  physical  characters, 
and  was  abandoned  after  an  improvement 
was  made  in  the  device  for  the  application  of 
coagulants.  It  is  too  expensive  for  regular 
use. 

Lime,  electrolytically  decomposed  salt  and 
metallic  iron  were  tried  experimentally  in  the 
Jewell  System,  but  were  abandoned. 

Preparation  of  Chemical  Soli/lions. — The 
first  Western  device  was  a  failure.  In  all 
other  cases  the  addition  of  known  weight  of 
chemicals  to  known  volumes  of  water  was  sat 
isfactory  when  it  received  sufficient  care  and 
attention. 

Application  of  Coagulant. — The  first  West 
ern  device  was  a  failure.  Experience  showed 
that  the  Warren  device  was  most  nearly  auto 
matic  and  011  the  whole  did  the  best  work 
under  these  conditions.  Satisfactory  results 
were  obtained  from  the  Jewell  and  second 
Western  devices  when  they  received  sufficient 
attention  and  regulation. 

It  is  quite  probable  that  in  practice  the 
most  satisfactory  results  could  be  obtained  by 
gravity  discharge  of  the  solutions. 

The  use  of  iron  pipes,  fittings  and  pumps 


SUMMARY  AND  DISCUSSION  OF  DATA    OF   1895-96. 


273 


to  handle  solutions  of  sulphate  of  alumina  is 
not  admissible.  Brass  and  aluminum  bronze 
were  not  attacked. 

Quantity  of  Coagulant  Used. — The  sum 
maries  already  presented  show  that  the  grains 
of  sulphate  of  alumina  used  per  gallon  of  net 
filtered  water  in  the  case  of  the  several  sys 
tems  were  as  fojlows: 

Warren.     Jewel..       «££" 

10.86       12.60 


i .  10 

2.72 


The  available  information  indicates  that  the 
river  water  during  these  tests  was  somewhat 
easier  to  purify  by  these  systems  than  would 
be  the  average  water  year  by  year.  There 
fore  it  is  concluded  that  in  no  case  would  any 
of  these  systems  treat  the  water  with  less  than 
an  annual  average  of  at  least  3  grains  per  gal 
lon  of  ordinary  sulphate  of  alumina. 

The  Period  of  Coagulation. — The  effective 
period  of  coagulation  in  minutes  at  the  con 
tract  rate,  including  the  settling  basins  and 
the  compartments  in  the  niters  above  the  sand 
layers,  was  in  each  case  as  follows: 


In  no  case  were  provisions  made  to  allow 
a  division  to  be  made  in  the  application  of  the 
coagulant  to  allow  favorable  conditions  for 
coagulation  and  subsidence,  and  of  coagula 
tion  and  nitration.  It  appears  that  at  times 
this  will  be  necessary. 

None  of  the  above  periods  with  a  single 
point  of  application  of  coagulant  would  be 
advisable  in  practice.  At  times  they  ought 
to  be  much  longer.  In  this  connection  it  may 
be  noted  that  the  value  of  secondary  applica 
tion  of  coagulant  was  appreciated  by  the  op 
erators  of  the  Warren  System,  as  shown  by  its 
trial  of  July  22,  under  the  conditions  which 
were  available. 

Coagulation  and  Sedimentation. — As  noted 
above,  coagulation  and  sedimentation,  inde 
pendent  of  coagulation  and  filtration,  would 
be  a  great  benefit  at  times,  but  was  not  pro 
vided  in  any  of  the  systems,  although  its  im 
portance  was  recognized  by  the  operators  of 
the  Warren  System. 

Inspection  and  Cleaning  of  Settling  Basins. — 
No  adequate  arrangements  in  this  particular 


were  made  in  any  of  the  systems,  although 
the  Jewell  was  superior  to  the  others. 

Coagulation  of  Water  on  Sand  Layer. — This 
is  a  point  of  great  practical  importance  and 
depends  upon  t'he  quantity  of  coagulant  and 
provisions  for  coagulation  and  sedimentation. 
The  latter  points  are  mentioned  above. 

Structure  and  Type  of  Filter. — The  use  of 
wood  in  a  permanent  plant  would  not  be  ad 
visable,  although  for  experimental  purposes 
wood  suffices.  In  this  respect  the  Western 
pressure  filter  was  superior.  The  disadvan 
tage  of  wood  was  shown  by  the  foul  odors  in 
the  filtered  water  compartment  at  the  bottom 
of  the  Warren  filter. 

Compared  with  pressure  systems  the  grav 
ity  filters  were  found  to  be  more  practicable 
for  the  purification  of  this  class  of  water  under 
ordinary  circumstances. 

The  location  of  the  sand  layer  near  the  top 
of  the  filtered  tank,  and  the  use  of  a  negative 
pressure,  as  in  the  case  of  the  Jewell  filter,  was 
a  distinct  advantage  in  that  it  reduced  the 
wasting  of  coagulated  but  unfiltered  water 
above  the  sand  layer  at  times  of  wasting  and 
similar  operations.  In  other  respects  no  ad 
vantages  of  a  negative  pressure  were  noted. 

In  practice  all  important  parts  should  be 
made  as  accessible  as  possible,  and  in  this  re 
spect  several  modifications  in  all  the  filters 
could  be  made  to  advantage. 

Sice  of  Filters. — All  of  the  filters  were  built 
to  purify  250,000  gallons  per  twenty-four 
hours,  and  this  size,  and,  so  far  as  our  knowl 
edge  goes,  this  is  the  prevailing  one  in  prac 
tice.  On  a  large  scale  the  cost  of  construc 
tion  and  of  operation  with  regard  to 
attendants  could  be  materially  reduced  by 
increasing  the  size  of  the  filters.  The  limit  in 
size,  apparently,  would  be  determined  by  the 
arrangements  for  successful  agitation. 

In  this  connection  it  is  said  that  the  Jewell 
Company  is  now  building  large  filters. 

Sand  Layer. — The  data  upon  this  point  are 
so  obscured  by  other  factors  that  it  is  difficult 
to  compare  them  fairly.  The  indications  are 
that  the  Warren  sand  layer  was  too  coarse 
and  that  the  greater  frictional  resistance  of 
the  Western  pressure  sand  layer  made  other 
operations  much  more  nearly  satisfactory 
mdcr  the  existing  conditions  than  would  have 
')een  the  case  had  a  coarser  sand  been  em- 


274 


WATER   PURIFICATION  A 7^  LOUISVILLE. 


ployed.  This  observation  is  based  upon  the 
comparative  freedom  from  fine  particles  of 
aluminum  hydrate  in  the  effluent  of  this  filter 
in  the  presence  of  irregular  coagulation  of 
the  applied  water  (see  Chapter  III).  Whether 
it  would  be  better  to  use  a  greater  thickness  of 
layer  or  finer  sand,  to  secure  increased  fric- 
tional  resistance,  is  not  plain.  The  latter 
would  probably  be  advisable,  as  it  would  not 
increase  the  cost  of  construction. 

The  sand  layer  of  the  Jewell  filter  gave  the 
best  results  under  the  existing  conditions,  but 
in  the  opinion  of  the  writer  it  would  be  better 
to  use  an  equal  depth  of  finer  sand. 

There  were  no  indications  that  crushed 
quartz  was  distinctly  superior  to  the  cheaper 
natural  sand. 

Filtered-water  Exits. — To  secure  a  uniform 
and  regular  rate  of  flow  of  water  through  the 
sand  layer,  the  exit  area  for  the  filtered  water 
and  the  inlet  area  for  the  wash-water,  at  the 
bottom  of  the  sand  layer,  should  apparently  be 
less  than  that  of  the  main  pipe  beneath  them. 
In  respect  to  this  condition  the  Jewell  filter 
alone  fulfilled  it.  It  would  seem  advisable, 
however,  to  decrease  the  distance  between 
the  strainer  cups  to  secure  more  uniform  flow 
in  the  lower  portion  of  the  sand  layer. 

The  Western  exit  devices  were  very  poor, 
because  in  the  slotted  tubes  sand  accumulated 
in  a  short  time. 

So  far  as  could  be  noted,  the  exits  of  the 
Warren  filter  served  their  purpose  fairly  well, 
but  the  varying  space  occupied  beneath  them 
by  the  supporting  frame  was  undesirable. 

In  no  case  were  these  portions  accessible 
without  removing  the  sand. 

Loss  of  Head. — The  indications  were  that 
about  TO  feet  of  maximum  available  head,  as 
ordinarily  utilized  in  the  Jewell  filter,  was  best. 
Amounts  above  this,  as  in  the  Western  pres 
sure  filter,  could  be  used  too  seldom  to  be 
advisable.  In  the  Warren  filter  not  more  than 
4  feet  were  used,  owing  chiefly  to  the  coarse 
ness  of  the  sand  layer. 

With  regard  to  pressure  filters  and  negative 
head,  see  foregoing  remarks  on  types  of  fil 
ters. 

Rate  of  Filtration. — There  are  no  indica 
tions  that  it  would  be  advisable  to  employ 
rates  of  less  than  100  million  gallons  per  acre 
daily,  and  it  is  quite  possible  that  this  limit 


could  be  safely  raised.  The  data,  however, 
are  too  complicated  by  other  factors  to  make 
this  a  decisive  conclusion.  But  it  is  probable 
in  view  of  the  results  from  the  Western  pres 
sure  filter  that  in  practice  under  favorable 
conditions  the  plant  could  be  operated  so  as 
to  make  increased  (uniform)  rates  in  a 
measure  meet  increased  demands  for  filtered 
water. 

Regulation  and  Control. — This  is  an  im 
portant  point  both  with  regard  to  necessity 
of  uniform  rate  to  give  satisfactory  results 
and  also  in  respect  to  cost  of  operation. 
The  automatic  controller  of  the  Jewell  filter 
was  very  crude,  but  a  step  in  the  right  direc 
tion. 

}Vashing  the  Sand  La\cr. — Thorough  wash 
ing  of  the  sand  layer  is  very  important.  To  se 
cure  this  it  is  necessary  to  distribute  the  wash- 
water  uniformly  under  the  sand  layer.  In  this 
respect  the  Jewell  filter  was  the  most  satisfac 
tory,  though  as  mentioned  before  a  smaller 
distance  between  the  cups  seems  desirable. 

Agitation  of  the  sand  layer  during  washing 
was  an  advantage  as  shown  by  the  operation 
of  the  Warren  and  Jewell  filters.  Of  the  two 
agitating  devices,  that  of  the  Jewell  filter  was 
less  cumbersome  and  did  not  move  the  sand 
from  the  center  toward  the  periphery.  It 
worked  poorly  at  times,  apparently  due  to  a 
binding  of  the  gears  occasioned  by  the  warp 
ing  of  the  partly  submerged  timbers  upon 
which  the  agitator  rested.  Both  the  Warren 
and  Jewell  devices  lacked  simplicity  of  detail 
and  were  too  weak  for  the  purpose.  These 
defects  could  and  should  be  remedied. 

Surface  Agitation. — This  procedure  to  re 
lieve  clogging  was  used  in  the  Jewell  filter 
and  was  a  decided  step  in  advance.  Its  suc 
cess  is  associated  closely  with  the  degree  of 
coagulation  of  the  water  entering  the  sand 
layer,  the  character  of  the  sand  layer  and  the 
arrangement  of  the  tank  containing  the  sand 
layer.  The  successful  employment  of  this 
method  could  probably  be  extended  by  a 
modification  of  the  above  factors. 

Steaming. — This  did  not  seem  to  be  neces 
sary  during  these  tests,  although  it  might  be 
the  case  in  some  instances.  This  disadvantage 
of  it  is  that  it  makes  the  organic  matter  on 
the  sand  serve  as  a  better  food  for  micro 
organisms. 


SUMMARY  AND  DISCUSSION   OF  DATA    OF   1895-96. 


275 


Quality  of  the  Filtered  Ohio  River  Water. 

With  proper  attention  to  the  operation 
of  the  systems,  and  an  adequate  degree  of 
coagulation  of  the  water  as  it  entered  the 
sand  layer,  these  systems  could  produce  a 
quality  of  filtered  water  which  would  be  thor 
oughly  satisfactory  under  all  ordinary  con 
ditions  with  regard  to  appearance  and  sani 
tary  character. 

From  an  industrial  standpoint,  the  filtered 
water  would  have  a  greater  corroding  action 
upon  uncoated  iron  receptacles  but  not  upon 
lead  pipe;  and  it  would  contain  more  incrust- 
ing  constituents  when  used  in  steam  boilers. 
Concerning  this  last  point  the  total  quantities 
would  not  be  excessive,  compared  with  aver 


age  Western  waters,  and  the  removal  of  the 
suspended  matters  would  largely  if  not  wholly 
offset  the  added  sulphate  of  lime. 

Owing  to  inherent  qualities  of  the  Ohio 
River  water,  the  storage  of  the  effluent  in  open 
reservoirs  in  this  climate  would  require  very 
careful  consideration,  and  the  period  could 
not  be  a  long  one,  owing  to  conditions  favor 
ing  growths  of  alga?,  etc. 

Final  Conclusions. 

In  all  these  systems  the  provision  for  sub 
sidence,  both  with  and  without  coagulation, 
was  thoroughly  inadequate  in  each  case;  but 
with  regard  to  filtration  proper  the  Jewell  fil 
ter  was  the  most  satisfactory. 


276 


WATER   PURIFICATION  AT  LOUISVILLE. 


CHAPTER  X. 

DESCRIPTION    OF    THE    HARRIS    MAGNETO- ELECTRIC  SYSTEM  OF  PURIFICATION,  AND  A 
RECORD    OF   THE   RESULTS  ACCOMPLISHED   THEREWITH. 


THIS  system  consisted  essentially  of  a  series 
of  large,  iron-covered  tanks,  and  a  set  of 
electrical  and  magnetic  appliances.  Accord 
ing  to  the  terms  of  the  contract  this  experi 
mental  system  was  to  have  a  capacity  of  250,- 
ooo  gallons  per  twenty-four  hours.  A  brief 
general  description  of  the  system  is  as  fol 
lows  : 

On  the  inlet  water-pipe  there  was  a  small 
iron  cylinder  with  a  porcelain  lining.  As  the 
water  passed  through  this  cylinder,  called  a 
spark  drum,  it  met  the  discharge  of  an  electric 
current  of  high  voltage.  From  this  cylinder 
the  water  passed  in  succession  through  three 
large,  round  iron  tanks  with  conical  bottoms. 
Each  of  these  tanks  contained  a  lining  for  the 
purpose  of  insulation.  The  water  entered  each 
of  these  tanks,  in  turn,  at  the  side  about  two 
feet  from  the  top.  In  the  upper  portion  of 
the  tanks  were  electrodes  between  which  the 
water  flowed  as  it  passed  out  of  the  tanks  at 
the  top.  On  the  top  of  each  of  the  tanks  was 
a  set  of  electro-magnets.  The  outlet  pipe  con 
nected  with  an  opening  in  the  cover  and  be 
tween  the  magnets.  The  three  tanks  were 
similar  in  construction,  and  the  outlet  pipes 
from  the  first  two  tanks  entered  the  second 
and  third  tanks,  respectively. 

The  fundamental  principles  upon  which 
this  system  was  based  were  never  accurately 
explained  to  me.  Electro-chemical  action 
was  considered  to  be  an  important  factor  in 
connection  with  the  destruction  of  the  bac 
teria  and  organic  matter  in  the  water.  It  was 
intended  tha^all  suspended  matter  would  be 
repelled  by  the  action  of  the  magnets  situated 
at  the  top  of  the  three  tanks;  and  the  mag 
nets  were  to  force  the  suspended  matters, 
including  the  bacteria,  to  the  bottom  of  the 
tanks,  where  pipes  leading  to  the  sewer  were 
provided. 


There  will  next  be  presented  a  more  de 
tailed  description  of  these  devices  and  the  ac 
companying  electrical  machines  and  appli 
ances.  Before  doing  so,  however,  it  is  to  be 
recorded  that,  owing  to  delays  in  the  prepara 
tion  of  castings,  etc.,  the  construction  of  this 
system  was  not  begun  until  March  27,  1896. 
No  official  attention  from  the  laboratory  was 
given  to  the  system  until  June  24.  A  large 
portion  of  the  intervening  period  of  three 
months  was  occupied  in  improvements, 
especially  with  regard  to  an  insulating  lining 
for  the  three  large  iron  tanks,  as  will  be  ex 
plained  beyond. 


The  spark  drum,  at  the  beginning  of  the 
system,  was  a  cast-iron  cylinder  of  a  special 
design.  It  was  18  inches  long  and  10  inches 
in  diameter.  Near  each  end  on  opposite  sides, 
a  branch  was  taken  off  to  connect  with  the 
inlet  and  outlet  water-pipes,  respectively.  The 
cylinder  and  branches  were  one  casting  and 
were  all  lined  with  porcelain.  The  ends  were 
closed  with  caps  which  were  bolted  on  to  the 
drum.  At  the  center  of  each  end  there  was 
a  stuffing  box,  through  which  there  were 
passed,  respectively,  the  two  pole  pieces  of 
the  high  voltage  circuit  from  a  Ruhmkorff 
coil.  When  the  system  was  in  operation  these 
pole  pieces  were  said  to  be  3  inches  apart. 

Iron   Tanks  containing  the  Electrodes  and 
Electro-magnets. 

These  tanks,  three  in  number,  were  made 
of  cast  iron,  i  inch  in  thickness.  The  upper 
half  of  each  tank  was  cylindrical  in  form,  and 
the  lower  half  was  in  the  form  of  a  cone  with 
the  apex  at  the  bottom. 


HARRIS  MAGNETO-ELECTRIC  SYSTEM  OF  PURIFICATION. 


277 


The  inside  dimensions  were  as  follows:  Di 
ameter  of  cylinder,  35.5  inches;  depth  of 
cylinder,  36  inches;  depth  of  cone,  36  inches; 
and  diameter  of  opening  at  the  apex  of  the 
cone  (bottom  of  the  tank),  3  inches.  This 
opening  at  the  bottom  of  the  tank  connected 
with  a  pipe  which  led  to  the  sewer.  Brass 
covers  closed  the  top  of  the  tanks,  and  sup 
ported  the  electro-magnets  in  the  manner  de 
scribed  below.  The  tanks  were  placed  on 
suitable  pedestals. 

The  lining  of  the  tanks  was  originally  of 
cement.  This  did  not  give  satisfactory  insu 
lation  and  at  the  time  that  the  system  was  ex 
amined  officially  the  tanks  were  lined  with  soft 
rubber  sheets. 

The  inlet  water  pipes,  3  inches  in  diameter, 
entered  at  the  side  of  the  tanks,  2  feet  from 
the  top.  The  opening  for  the  inlet  pipe  was 
lined  with  porcelain.  A  porcelain  hood,  0.625 
inch  thick,  3  inches  in  diameter  and  4  inches 
long,  was  provided  at  the  inlet  opening  to 
break  the  currrent  of  the  water.  At  the  apex 
of  the  conical  bottom  of  the  tanks  there  was 
a  3-inch  opening  which  connected  with  a  3- 
inch  pipe  leading  to  the  sewer.  Plug  valves 
controlled  the  flow  through  these  blow-off 
pipes.  The  main  exits  from  the  tanks  were 
openings  in  the  covers;  and  into  cast-iron 
chambers  on  these  covers  were  connected 
the  outlet  water  pipes,  3  inches  in  diameter. 

Electro-magnets. — On  the  brass  casting,  i 
inch  in  thickness,  which  formed  the  cover  of 
each  tank,  there  rested  a  set  of  5  electro 
magnets.  In  the  center  there  was  a  large 
one,  15  inches  in  diameter,  with  a  core  of  12 
inches.  Four  small  magnets,  each  8  inches  in 
diameter  with  a  core  of  6  inches,  surrounded 
the  central  one.  The  core  of  the  large  central 
magnet  passed  through  an  opening  in  the 
brass  cover  and  was  fastened  on  the  under 
side  to  an  iron  disc  if>  inches  in  diameter  and 
r  inch  thick,  which  formed  the  negative  pole. 
The  cores  of  the  four  outer  magnets  passed 
through  the  brass  plate  and  connected  with 
an  iron  ring  on  the  under  side,  which  formed 
the  positive  pole.  This  ring  was  10  inches 
wide  and  i  inch  thick.  Between  the  disc  and 
the  ring  was  a  circular  opening  0.25  inch  wide 
and  16  inches  in  diameter.  Communication 
with  the  outlet  recess  on  the  top  of  the  cover 
was  obtained  by  a  number  of  small  holes 


drilled  through  the  brass  cover  just  above 
this  circular  opening. 

The  magnets  were  connected  at  the  upper 
end  by  a  cast-iron  cross  about  6  inches  thick. 
With  a  full  current  from  the  generator  (45 
amperes)  the  lifting  force  of  each  set  of  (5) 
magnets  was  said  to  be  about  6  tons. 

Electrodes. — The  size  and  arrangement  of 
the  electrodes  were  changed  a  number  of 
times  during  the  period  covered  by  the  pre 
liminary  trials  of  the  system.  On  the  date  of 
the  official  examination  the  positive  electrode 
consisted  of  a  series  of  pressed  carbon  plates. 
The  plates  were  o.25-inch  in  thickness  and 
12  inches  in  width.  They  were  placed  in  a 
parallel  and  vertical  position,  and  suitable  in 
sulation  and  support  were  provided  to  keep 
them  about  i  inch  apart.  The  lengths  of  the 
carbon  plates  varied  with  the  length  of  the 
parallel  chords  which  they  formed  with  the 
periphery  of  the  tank,  respectively.  The  total 
area  of  these  plates  (one  side)  was  about  96,- 
ooo  square  inches. 

The  top  of  the  carbon  plates  was  about  6 
inches  below  the  brass  top  of  the  tanks.  From 
the  bottom  of  the  plates  to  the  plane  in  which 
the  water  entered  the  tanks  the  distance  was 
6  inches. 

The  negative  pole  was  placed  near  the  bot 
tom  of  the  tanks.  It  was  a  small  sheet  of 
metallic  aluminum  about  0.06  inch  in  thick 
ness,  and  about  150  square  inches  in  area. 

Suitable  openings  in  the  tanks  were  pro 
vided  for  the  connection  of  the  wires  to  the 
electrodes. 

Piping.- — The  inlet  and  outlet  pipes  of  the 
spark  drum  were  4  inches  in  diameter.  With 
this  exception  all  the  piping,  including  inlet, 
and  blow-off  pipes  of  the  respective  tanks, 
was  3  inches  in  diameter.  The  outlet  pipe 
from  the  third  and  last  tank  led  to  a  con 
denser  where  the  exhaust  steam  from  the  en 
gine  which  operated  the  generator  was  con 
densed. 

All  of  the  tanks  and  also  the  spark  drum 
were  closed  compartments.  The  rate  of  flow 
of  water  through  the  system  was  controlled 
by  a  valve  on  the  main  inlet  pipe  which  con 
tained  the  river  water  under  about  fio  pounds 
pressure.  Suitable  valves  were  also  provided 
on  the  inlet  and  outlet  pipes  of  each  tank. 

The  blow-off  pipes  at  the  bottom  of  each 


WATER   PURIFICATION  AT  LOUISVILLE. 


tank  were  3  inches  in  diameter  and  connected 
directly  with  the  sewer.  The  flow  through 
these  pipes  was  controlled  by  3-inch  plug 
valves. 

Engine. — A  simple  stationary  engine  was 
used  to  drive  the  generator.  Its  principal 
dimensions  were  as  follows:  Diameter  of 
steam  cylinder,  9.25  inches;  length  of  stroke, 
8.75  inches;  and  cut-off,  70  per  cent.  The 
fly-wheel  and  driving-pulley  were  combined, 
and  had  a  diameter  of  4  feet  and  a  rim  12.5 
inches  in  width.  Its  weight  was  about  1200 
pounds. 

From  the  engine  the  power  was  conveyed 
to  the  generator  a  distance  of  about  20  feet, 
by  means  of  a  leather  belt  6  inches  wide. 

Dynamo-generator. — The  generator  was  a 
compound-wound,  bi-polar  machine.  It  was 
wound  to  generate  a  direct  current  of  220 
volts  and  45  amperes,  at  a  speed  of  1 125  revo 
lutions  per  minute.  The  driving  pulley  was 
8.75  inches  in  diameter  and  6  inches  wide.  A 
rheostat  was  provided  to  regulate  the  inten 
sity  of  the  field  by  regulating  the  amount  of 
current  passing  through  the  shunt  winding. 
It  was,  however,  seldom  used. 

Electric  Circuits. — At  the  switch-board  the 
main  circuit  was  divided  into  three  principal 
sub-circuits.  The  first  of  these  sub-circuits 
passed  directly  to  the  electro-magnets  situ 
ated  on  top  of  the  tanks;  the  second  led  to 
the  electrodes  within  the  tanks;  and  the  third 
passed  through  an  interrupter  to  a  Ruhm- 
korff  coil  from  which  the  induced  current  of 
high  voltage  passed  to  the  spark  drum.  All 
of  these  circuits  were  arranged  in  parallel  on 
the  main  circuit.  A  fourth  sub-circuit  was 
also  taken  off  to  a  small  electric  motor  which 
turned  the  interrupter  on  the  third  circuit. 

Resistance  coils  were  used  to  control  the 
electric  current.  They  were  made  of  50  coils 
of  No.  14  galvanized  iron  wire,  about  4000 
feet  in  all  being  used.  Connections  were 
made  so  that  any  number  of  coils  could  be 
used  as  desired. 

Results  Accomplished  by  the  Harris  Magneto- 
electric  System. 

This  system  was  in  official  operation  only 
for  one  hour,  from  4.00  to  5.00  P.M.  on  June 


24, 1896.  The  record  of  its  operation,  with  the 
results  of  analyses  of  the  river  water  before 
and  after  passage  through  the  system,  is  as 
follows: 

The  rate  at  which  the  water  passed  through 
the  full  system  was  gradually  increased  until 
at  4.10  P.M.  it  had  reached  23.5  cubic  feet  per 
minute,  equivalent  to  254,000  gallons  per  24 
hours.  For  ten  minutes  this  rate  was  held 
approximately  constant.  At  the  end  of  this 
time,  4.20  P.M.,  samples  of  water,  the  an 
alyses  of  which  appear  in  the  next  tables,  were 
collected  as  follows: 

Bacterial  sample  Xo.  3959  was  taken  from 
the  water  as  it  left  the  spark  drum. 

Bacterial  sample  No.  3960  was  taken  from 
the  water  as  it  left  the  last  tank. 

Chemical  sample  No.  671  was  taken  from 
the  water  which  was  "  blown  off  "  at  the  bot 
tom  of  the  tanks. 

Chemical  sample  No.  672  was  taken  from 
the  water  as  it  left  the  last  tank. 

For  the  next  ten  minutes  the  average  rate 
of  flow  of  the  water  through  the  entire  sys 
tem  was  16.5  cubic  feet  per  minute,  equiv 
alent  to  178,000  gallons  per  24  hours. 

At  the  end  of  this  time,  4.30  P.M.,  the  fol 
lowing  samples  were  collected  for  analysis: 

Bacterial  sample  No.  3961  was  taken  from 
the  water  as  it  left  the  spark  drum. 

Bacterial  sample  No.  3962  and  chemical 
sample  No.  673  were  collected  from  the  water 
which  had  passed  through  the  entire  system. 

During  the  next  period  of  fifteen  minutes 
there  was  maintained  an  average  rate  of  flow 
of  12.5  cubic  feet  per  minute,  equivalent  to 
105,000  gallons  per  24  hours.  At  4.45  P.M. 
samples  corresponding  to  those  noted  above 
were  taken  as  follows: 

Bacterial  sample  No.  3968  was  collected 
from  the  water  after  passage  through  the 
spark  drum. 

Bacterial  sample  No.  3969  and  chemical 
sample  No.  674  were  collected  from  the  water 
after  passage  through  the  entire  system. 

From  4.45  to  5.00  P.M.  the  average  rate  of 
flow  of  water  through  the  system  was  6.2 
cubic  feet  per  minute,  equivalent  to  67,000 
gallons  per  24  hours.  The  following  samples 
were  collected  at  5.00  P.M.  which  was  the  end 
of  the  test  of  this  system. 


HARRIS  MAGNETO-ELECTRIC   SYSTEM  OF  PURIFICATION. 


279 


purification    of   the    water   after   its    passage 
through  the  system. 

This  system  was  never  put  in  official  opera 
tion  after  this  date.  Various  portions  of  it, 
however,  were  utilized  in  the  devices  which 
were  operated  by  the  Harris  Company  during 
the  following  month. 

RESULTS  OF  BACTERIAL  ANALYSES  OF  SAMPLES 
DESCRIBED    ABOVE. 


Bacterial  sample  No.  3971  was  collected 
from  the  water  after  passage  through  the 
spark  drum. 

Bacterial  sample  No.  3970  and  chemical 
sample  Xo.  675  were  collected  from  the  water 
after  passage  through  the  entire  system. 

At  4.44  P.M.  chemical  and  bacterial  samples 
of  the  river  water,  having  the  following  num 
bers,  respectively,  679  and  3963,  were  col 
lected  for  analysis. 

The  electric  current,  during  the  period 
from  4.00  to  5.00  P.M.,  June  24,  had  an  aver 
age  voltage  of  206  and  an  amperage  of  20  to 
21.  as  it  left  the  generator  on  its  way  to  the 
full  system  which  was  in  use  at  this  time. 

In  the  next  table  are  presented  the  results 
of  analyses  of  the  several  samples  of  water  de 
scribed  above.  They  show  no  appreciable 


RESULTS   OF   CHEMICAL   ANALYSES   OF   SAMPLES    DESCRIBED   ABOVE. 
(Parts  per  Million.) 


Number  of 
Sample. 

Source  of  Sample. 

Collected  June 
24.     Hour. 

Bacteria  per 
Cub.  Centimeter. 

3959 

Spark  Drum 

4.2O  P.M. 

10  400 

3960 

Effluent 

4.20 

II  800 

3961 

Spark  Drum 

4  30 

7  600 

3962 

Effluent 

4.30 

10  100 

3963 

River 

4.44 

II  fioo 

3968 

Spark  Drum 

4  45 

13  100 

3969 

Effluent 

4-45 

8  800 

3970 

Effluent 

5.00 

9  Soo 

3971 

Spark  Drum 

5.00 

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O.  IO 

t  "  Blow-off  "  at  bottom  of  tanks.  J  Effluent. 


280 


WATER   PURIFICATION  AT  LOUISVILLE. 


CHAPTER  Xi. 

DESCRIPTION   OF  THE  DEVICES   OPERATED   BY  THE  HARRIS  COMPANY  IN  JULY,  AND  A 
RECORD    OF   THE   RESULTS   ACCOMPLISHED  THEREWITH. 


DURING  the  month  of  July,  1896,  a  num 
ber  of  devices,  more  or  less  alike,  were  oper 
ated  by  the  Harris  Company  with  the  view 
to  purifying-  the  Ohio  River  water.  Various 
portions  of  the  original  system  were  utilized 
in  the  several  devices,  as  will  appear  in  the 
descriptions  beyond  where  they  are  taken  up 
in  turn. 

The  devices  of  July  appeared  to  be  based 
mainly,  as  I  understand  the  matter,  on  the 
results  of  some  experiments  made  in  a  small 
glass  jar  during  the  last  week  in  June.  These 
experiments  may  be  summarized  briefly  as 
follows: 


A  glass  jar,  of  about  one  gallon  capacity, 
was  rilled  about  three-fourths  full  of  river 
water,  and  in  the  water  were  placed  two  cir 
cular  strips  of  aluminum  sheet.  The  thick 
ness  of  the  aluminum  sheets  was  about  0.06 
inch.  The  two  strips  were  separated  from 
each  other  by  suitable  blocks  of  an  insulating 
material,  about  0.125  mcn  thick.  The  cross 
section  of  the  electrolyte  (equal  to  the  area 
of  one  side  of  one  of  the  strips)  was  about 
30  square  inches. 

Through  these  electrodes  there  was  passed 
a  current  of  electricity  from  the  generator.  A 
considerable  quantity,  of  gas,  practically  all  of 
which  was  hydrogen,  was  set  free  at  the  nega 
tive  pole  by  the  action  of  the  current.  There 
was  formed  a  white  gelatinous  substance 
which  appeared  for  the  most  part,  if  not 
wholly,  at  the  positive  pole.  It  was  found 
that  this  substance  was  aluminum  hydrate. 
This  is  the  same  compound  that  is  formed  by 
the  decomposition  of  alum  or  sulphate  of 
alumina  by  lime,  as  has  been  explained  in  pre 
ceding  chapters. 


The  aluminum  hydrate  coagulated  the  sus 
pended  matters  in  the  water,  in  a  similar  man 
ner  as  when  sulphate  of  alumina  was  added  to 
the  water.  Instead  of  the  coagulated  masses 
subsiding  at  the  bottom,  as  in  the  application 
of  sulphate  of  aiumina,  the  greater  part  of 
them  were  carried  to  the  surface  by  the  rising 
currents  of  hydrogen  gas. 

When  the  electric  current  was  turned  off 
a  portion  of  the  matters  suspended  through 
out  the  water  settled  to  the  bottom  of  the  jar, 
while  some  of  them  joined  the  thick  scum 
which  formed  on  the  surface  of  the  water.  At 
the  end  of  a  few  minutes,  five  or  less,  the  main 
bulk  of  the  water  became  quite  clear,  with 
the  exception  of  a  few  scattering  particles  of 
aluminum  hydrate. 

With  regard  to  the  length  of  time  necessary 
to  coagulate  and  clarify  the  water,  this  de 
pends  upon  the  strength  (amperage)  of  the 
electric  current.  The  reason  of  this  lies  in 
the  fact  that  it  is  the  strength  of  the  current 
which  determines  the  rate  of  conversion  of 
metallic  aluminum  into  the  form  of  aluminum 
hydrate,  disregarding  any  secondary  solvent 
action  of  the  initial  compounds.  In  the  ex 
periments  which  received  official  attention 
the  current  was  applied  for  5  and  10  minutes, 
respectively.  It  was  estimated  that  the 
amounts  of  aluminum  which  were  converted 
to  aluminum  hydrate  were  about  7  and  17 
grains  per  gallon,  respectively. 

By  the  aid  of  a  siphon  portions  of  the  clari 
fied  water  were  removed  from  the  jar  for 
analysis.  The  bacterial  results  showed  that 
the  numbers  of  bacteria  in  the  river  water 
ranged  from  8  100  to  n  600,  while  in  the 
clarified  water  from  the  jar  the  numbers  were 
6,  68,  and  120  per  cubic  centimeter,  respect 
ively.  Disregarding  the  scattering  particles 
of  aluminum  hydrate,  the  chemical  results 


DEI' ICES   OPERATED   B Y    'JJJE  HARRIS  COAJPAAY  JX  JULY. 


281 


showed  the  removal  of  all  the  suspended  or 
ganic  and  mineral  matters  present  in  the  river 
water;  and,  further,  that  there  had  been  an 
appreciable  reduction  in  the  organic  matter 
which  was  dissolved  in  the  water. 

STATUS  OF  THE  SITUATION  ON  JULY  i,  WITH 

REGARD  TO  THE  MAGNETO-ELECTRIC 

SYSTEM  AND  DEVICES. 

The  magneto-electric  system  having  been 
abandoned,  practically  speaking,  by  the  Har 
ris  Company  after  the  official  test  of  one  hour 
on  June  24,  there  were  operated  during  July 
several  devices  in  which  use  was  made  of  the 
principles  illustrated  by  the  jar  experiments 
described  above.  It  is  to  be  recorded  here 
that  aluminum  electrodes  were  known 
to  have  been  employed  by  others  for 
the  purification  of  certain  waters  at  a  date 
earlier  than  that  of  these  experiments.  But 
it  is  also  to  be  stated  that  the  Harris  Com 
pany  claimed  that  their  magnets  would  sup 
plement  and  increase  the  action  of  the  elec 
trodes;  and,  further,  that  the  magnets  would 
facilitate  the  clarification  of  the  coagulated 
water,  and,  perhaps,  do  away  with  the  neces 
sity  of  subsequent  filtration  through  sand. 

The  devices  operated  in  July  will  be  de 
scribed  in  turn,  together  with  the  results 
which  they  accomplished,  respectively. 

DEVICE  No.   i. 

The  first  device  was  offered  by  the  Harris 
Company  for  official  examination  on  July  9. 
It  consisted  essentially  of  a  closed  iron  tank 
lined  with  porcelain,  which  contained  a  set  of 
aluminum  electrodes.  At  the  bottom  of  the 
tank  was  placed  a  set  of  magnets.  After 
treatment  in  this  tank  the  water  passed  to  the 
top  of  a  small  stand  pipe,  through  which  it 
flowed  from  top  to  bottom,  and  thence  to  the 
sewer. 

The  Tank  in  which  the  Wafer  wax  Treated. 

The  tank  in  which  the  water  was  subjected 
to  electrolytic  action  was  a  small  cast-iron 
cylinder  surmounted  by  a  brass  dome.  It  was 
lined  with  porcelain.  The  principal  inside  di 
mensions  were:  Diameter  of  cylinder  and 


base  of  dome,  1.71  feet;  height  of  cylinder, 
2  feet;  and  height  of  dome,  i  foot. 

The  water  entered  this  tank  at  the  top  and 
passed  out  at  the  bottom,  from  which  point  it 
was  conveyed  to  the  top  of  the  stand  pipe. 

Electrodes. — Aluminum  sheets,  arranged  in 
the  form  of  a  manifold,  composed  the  elec 
trodes  which  were  placed  within  the  porce 
lain-lined  tank.  They  were  made  of  sheets 
of  about  0.06  inch  thick,  which  were  held  to 
gether  by  hard  rubber  bolts,  the  desired  dis 
tance  between  the  plates,  1.75  inches,  being 
maintained  by  the  use  of  hard  rubber  separa 
tors.  Alternate  sheets  of  metallic  aluminum 
in  the  manifold  formed  the  positive  and 
negative  poles,  respectively.  The  total  area 
of  active  electrode  surface  (anodes)  was  about 
2550  square  inches. 

Magnets.— The  magnets  were  similar  in 
their  arrangement  to  those  of  the  three  tanks 
of  the  original  system,  described  in  the  last 
chapter,  except  that  they  were  placed  on  the 
bottom  instead  of  the  top  of  the  tank.  There 
were  five  magnets  in  the  set.  The  central  one, 
forming  the  negative  pole,  was  8  inches  in 
diameter.  The  other  pole  was  formed  by 
four  smaller  magnets  of  a  diameter  of  4 
inches.  The  latter  were  placed  around,  and 
connected  with,  a  ring  which  surrounded  the 
central  magnet. 

Stand  Pipe. — The  stand  pipe,  into  which 
the  water  passed  after  treatment  in  the  iron 
tank,  consisted  of  a  single  1 2-foot  length  of 
iron  pipe.  Its  diameter  was  20  inches,  and 
both  ends  were  closed  by  caps.  At  four  equi 
distant  points  in  the  stand  pipe  there  were 
placed  tin  cones  each  12  inches  high  and  20 
inches  in  diameter.  At  the  apex  of  each  cone 
was  an  opening  i  inch  in  diameter,  through 
which  the  water  flowed  downward  in  its  pas 
sage  through  the  stand  pipe.  The  cones  were 
all  placed  with  the  apex  upward.  At  the  side 
of  the  tanks  were  four  openings,  one  above 
the  base  of  each  of  the  respective  cones.  These 
openings  connected  with  blow-off  pipes  lead 
ing  to  the  sewer.  The  main  exit  was  about 
3  feet  from  the  bottom. 

Piping. 

The  inlet  and  outlet  water  pipes  of  the  tank 
and  stand  pipe  were  i  inch  in  diameter.  River 
water  was  supplied  to  the  device  under  a  pres- 


282 


WATER   PURIFICATION  AT  LOUISVILLE. 


sure  of  about  60  pounds.  The  blow-off  pipes 
leading  to  the  sewer  were  0.50  inch  in  diam 
eter. 

Electrical  Machines  and  Appliances. 

The  engine  and  generator  were  the  same 
that  were  used  in  the  system  described  in  the 
preceding  chapter. 

The  circuits  were  similar  except  that  the 
interrupter  and  Ruhmkorff  coil  were  not 
used. 


This  device  was  in  operation,  officially, 
from  2.30  P.M.  to  5.00  P.M.  on  July  9.  In  that 
time  514  cubic  feet  of  water  passed  through 
it.  The  rate  of  flow  ranged  from  3  to  4  cubic 


feet  per  minute,  and  averaged  3.43  cubic  feet 
per  minute,  which  is  equivalent  to  37,000  gal 
lons  per  24  hours. 

The  amount  of  metallic  aluminum,  which 
was  converted  electrolytically  into  aluminum 
hydrate,  was  estimated  to  be  equivalent  to 
about  o.  10  grain  per  gallon  of  water  treated. 

Observation  on  the  electric  current  em 
ployed  in  the  operation  of  this  device  showed 
that  the  amperage  averaged  18.8  and  the 
voltage  211.  The  average  current  was  equiv 
alent  to  .0122  ampere-hour  per  gallon  and  the 
power  was  144  electric  H.P.  per  million  gal 
lons  of  water  treated  per  24  hours. 

Samples  of  water  for  chemical  and  bacterial 
analyses  were  collected  as  the  water  left  the 
stand  pipe  at  3.30  P.M.  and  4.30  P.M.,  after  the 
device  had  been  in  operation  i  and  2  hours, 
respectively. 


CHEMICAL   RESULTS— DEVICE    No.   1. 
Analyses    of    Samples    Described    Below. 

(Parts  per  Million.) 


Nitr 

3Ken 

R< 

sinu. 

Fixe 

d  Res 

due 

oi 

1 

as 

rt 

Ev; 

porat 

on. 

afte 

Igni 

ion. 

1 

1 

1 

A 

mr.m, 

E 

gl 

s 

u 

z 

Date. 

Hour. 

2% 

£ 

•S 

T3 

* 

| 

g 

| 

| 

> 

| 

> 

| 

> 

7. 

h 

U 

o 

$ 

3  C- 

5  '' 

£ 

u 

H 

1 

Q 

H 

Q 

| 

Q 

c 

71  1 

July  9 

9.30  A.M. 

26.0 

.25 

6.6 

.378 

.272 

.  106 

.030 

.002 

.6 

6.9 

sSq 

47" 

IIQ 

523 

436 

87 

56.0 

o.o 

30.70 

719 

"    9 

Av.  2  samples. 

•  15 

6.4 

.404 

.302 

.102 

.062 

.006 

•9 

7-1 

594 

475 

Ilq 

521 

435 

S6 

54.0 

o.o 

22.00 

The  two  corresponding  chemical  samples 
of  the  treated  water  were  mixed  together  and 
analyzed  as  sample  No.  719.  The  results  of 
the  analysis  of  this  sample  and  that  of  the 
river  water  on  that  day,  sample  Xo.  714,  col 
lected  at  9.30  A.M.,  are  given  above. 

The  results  of  bacterial  analysis  of  these 
samples  and  of  the  river  water  on  that  day 
are  as  follows: 


DEVICE  No.  2. 


BACTERIAL    RESULTS—  DEVICE    No.  1. 


Col 

ected. 

Hacieria 

Source  of  Sample. 

Date. 

1896. 

Hour. 

per  Cubic 

River  

July  9 

9.30  A.M. 

8  600 

River     

Treated  water  

"    9 

4-3"     " 

8  700 

No  substantial  purification  of  the  water  by 
this  device  is  shown  by  the  above  results. 
After  this  test  of  July  9  modifications  and  ad 
ditions  to  the  device  were  made. 


On  July  1 6  a  second  device  was  offered  for 
official  inspection.  It  was  simply  an  elabora 
tion  and  extension  of  the  first  device.  There 
were  added  two  duplicates,  practically  speak 
ing,  of  the  porcelain-lined  iron  tank  contain 
ing  electrodes  and  magnets  as  above  de 
scribed.  The  original  one  was  also  used, 
making  three  in  all.  The  total  area  of  active 
electrode  surface  (anodes)  was  about  4000 
square  inches,  and  the  distance  between  the 
plates  averaged  1.75  inches. 

To  facilitate  clarification  of  the  water  after 
the  treatment  in  these  tanks  there  were  used, 
in  addition  to  the  stand  pipe,  the  three  large 
iron  tanks  employed  in  the  original  system. 
The  flow  of  water  through  the  stand  pipe  was 
reversed  ;  that  is  to  say,  it  entered  at  the 
bottom  and  passed  out  at  the  top. 

In  the  passage  of  the  water  through  each 


DEVICES  OPERATED   BY    THE  HARRIS  COMPANY  IN  JULY. 


283 


of  these  seven  closed  vessels  successively,  it 
was  first  treated  in  the  three  porcelain-lined 
tanks  containing  the  electrodes  and  magnets; 
and  thence  it  passed  through  the  stand  pipe 
and  the  three  large  iron  tanks  for  clarification 
by  subsidence.  The  cubical  capacity  of  all 
the  vessels  was  about  126  cubic  feet,  as  fol 
lows:  each  of  the  three  porcelain-lined  tanks, 
5.5  cubic  feet;  stand  pipe,  26  cubic  feet;  each 
of  the  three  iron  tanks  of  the  original  sys 
tem,  28  cubic  feet;  and  piping  (i  and  3  inches 
in  diameter),  5  cubic  feet. 

Results  Accomplished  by  Device  No.  2. 

The  device  was  put  in  operation  on  the 
above-mentioned  date,  but  only  for  26  min 
utes  after  the  water  appeared  at  the  outlet 
pipe.  At  the  commencement  of  the  test  all 
the  tanks  and  the  stand  pipe  were  drained. 
Water  was  applied  at  11.52  A.M.,  and  first  ap 
peared  at  the  outlet  at  12.39  P-M-  The  opera 
tion  of  the  device  was  stopped  at  1.05  P.M. 

The  period  of  operation  was  too  short  to 
yield  any  decisive  information,  except  that 
there  was  no  improvement  in  the  appearance 
of  the  water  after  treatment  at  the  average 
rate  of  4  cubic  feet  per  minute. 


Samples  of  water,  before  and  after  treat 
ment,  were  collected  for  analysis,  and  the  re 
sults  are  presented  below  as  a  matter  of 
record.  It  will  be  noted  that  the  numbers  of 
bacteria  in  the  water  increased  during  the  pas 
sage  through  the  device.  The  reason  of  this 
appeared  to  be  that  there  were  accumulations 
on  the  walls  of  the  three  rubber-lined  tanks 
through  which  the  water  last  passed. 

BACTERIAL    RESULTS— DEVICE    No.  2. 


Source  of  Sample. 

Col 

ected. 

Bacteria 
per  Cubic 

Date. 

1896. 

Hour. 

M. 
M. 

River     . 

Ji: 

ly  16 
16 
16 
16 
16 
16 
16 
16 

9.30  A 
12.45  P 
12.50 
12.50 
12.55 
1  .00 
1.05 
5.00 

6  Soo 
22  900 

Treated  wa  < 
Treated  wa 
River   .  .    . 

5  600 
13700 
9  6co 
10  200 
5000 

Treated  wa 
Treated  wa 
Treated  wa 
River  

With  regard  to  the  following  results  of 
chemical  analyses,  sample  Xo.  740  was  col 
lected  from  the  river  water  at  12.50  P.M.; 
while  sample  No.  741  represents  a  mixture 
of  three  equal  portions  of  the  treated  water, 
collected  at  12.45  r-M-..  12.55  p-M->  and  1.05 
P.M.,  respectively. 


CHEMICAL    RESULTS— DEVICE  "No.  2. 
Analyses    of   Samples    Described    Above. 

(Parts  per  Million.) 


Nitr 

0 

Collected 

Fixed  Residue 

e 

as 

« 

Evaporation. 

after  Ignition. 

1 

z 

E 

Kg 

c 

Ammonia. 

i 

si 

Jj 

^ 

3 

z 

Date. 

Hour. 

i  M 

c 

•0 

•g 

£•£ 

S2 

u 

*D 

1 

•0 

13 

^ 

'S 

- 

1896. 

g-2 

g 

a       -3 

,  H 

•3 

S 

55 

?; 

"5 

•5 

£ 

i 

•g 

O. 

1 

i 

1 

^ 

(/I 

fi 

O 

O 

H 

in 

Q 

t 

0 

H 

1 

Q 

h 

3 

« 

Q        < 

Q 

i 

740 

Til 

July  16 

"     16 

12.50  I'.M. 
Av.  3  samples 

•27 
•  M 

7.0 

6.6 

.3^2 
•370 

.214 

.260 

.748 

.11' 

.030 
.044 

.000 

.012 

.6 
•  4 

2.2      540 

2  .  5    490 

404    136   480 
37o>  120    429 

404  76  52.7 
366  63   52.3 

o.o 
o.o 

15-40 
15.30 

DEVICE  No.  3. 

The  third  device  was  offered  for  official  in 
spection  on  July  1 8.  It  comprised  the  seven 
closed  vessels  described  as  the  second  device, 
and  in  addition  there  was  a  small  filter  of 
sand.  Concerning  the  portions  of  the  device 
common  to  the  second  one.  it  is  to  be  stated 
that  the  second  and  third  porcelain-lined  tanks 
were  used  only  as  settling  chambers.  Alu 
minum  electrodes,  the  anode  area  of  which  was 
about  2300  square  inches,  were  placed  only  in 


the  first  porcelain-lined  tank  where  the  river 
water  entered  the  device.  The  direct  use  of 
the  magnets  was  also  abandoned,  and  they 
were  used  only  as  resistance  coils  to  control 
the  current  and  prevent  the  passage  of  a 
greater  current  than  the  fittings  were  designed 
for.  The  water  passed  through  the  seven 
closed  vessels  in  the  same  order  as  in  the 
second  device.  When  the  water  reached  the 
last  tank  a  portion  of  it  was  passed  through 
the  filter. 


284 


WATER   PURIFICATION  AT  LOUISVILLE. 


Filter. 

The  filter  \vas  made  by  filling  with  sand  a 
galvanized  iron  tank,  which  was  2  feet  in  di 
ameter  and  3  feet  deep.  The  outlet  of  this 
tank  was  a  common  o. 5-inch  tap.  On  the 
bottom  of  the  tank  were  placed  three  pieces 
of  slotted  brass  pipe,  which  were  to  serve  as 
strainers  and  allow  the  water  to  pass  to  the 
outlet  tap  while  the  sand  was  kept  in  place. 
These  tubes  were  1.5  inches  in  diameter  on 
the  inside.  The  length  of  one  was  10  inches 
and  of  each  of  the  other  two  8  inches.  They 
were  all  screwed  into  a  cross  which  connected 
with  the  outlet  tap.  In  each  tube  there  were 
5  rows  of  circumferential  slots  which  aver 
aged  0.024  inch  in  width  and  0.72  inch  in 
length.  These  slots  were  spaced  about  0.125 
inch  from  center  to  center. 

Sand  Used. — Coarse  sand  of  an  effective 
size  of  0.56  millimeter  was  placed  on  the  bot 
tom  of  the  tank  to  a  depth  of  6  inches,  sur 
rounding  and  covering  the  slotted  tubes. 
Above  this  layer  of  sand  were  24  inches  of  a 
somewhat  liner  sand  having  an  effective  size 
of  0.51  millimeter.  The  surface  of  the  sand 
was  about  (>  inches  below  the  top  of  the  tank. 

Resistance  of  Strainers  and  Sand  Layer. — 
\Vith  the  sand  entirely  removed  from  the 
tank,  the  maximum  rate  at  which  the  strainer 
tubes  and  the  outlet  tap  allowed  water  to  flow 
was  0.37  cubic  feet  per  minute,  equivalent  to 
55  million  gallons  per  24  hours  per  acre  of 
tank  area.  \Yith  the  sand  in  place,  and  the 
surface  free  from  accumulations  of  suspended 
matter,  this  rate  was  0.28  cubic  foot  per  min 
ute,  equivalent  to  42  million  gallons  per  acre 
per  24  hours. 

Piping. — Suitable  piping  was  provided  to 
carry  a  portion  of  the  water,  as  it  passed 
through  the  outlet  of  the  last  tank,  to  the 
filter.  Connections  were  made  with  the  out 
let  pipe  so  that  purified  water  could  be  forced 
up  through  the  sand  for  the  purpose  of  wash 
ing.  The  sand  was  stirred  by  hand  during 
the  process  of  washing. 


This  device  was  operated  during  four  hours 
on  July  18.     At  10.05  A.M.  operation  was  be 


gun,  with  the  tanks  and  filter  empty.  River 
water  was  applied  to  the  device  at  a  rate  of 
about  3.0  cubic  feet  per  minute.  The  full  set 
of  (seven)  tanks  was  filled  with  water  at 
10.47  A-M-  ^t  triat  t'1116  water  from  the  outlet 
of  the  last  tank  was  applied  to  the  filter.  The 
rate  of  Mow  of  water  through  the  tanks  was  then 
increased  to  about  5  cubic  feet  per  minute.  For 
the  greater  part  of  the  time  the  water  passed 
through  the  filter  at  about  the  maximum  rate; 
and  observations  showed  this  to  be  from  o.  16 
to  O._M  cubic  foot  per  minute,  equivalent  to 
24  and  31  million  gallons  per  acre  per  24 
hours,  respectively.  After  12.05  [VM-  tne 
water  passed  through  the  tanks  at  an  average 
rate  of  about  1.3  cubic  feet  per  minute,  equiv 
alent  to  14,000  gallons  per  24  hours.  The  op 
eration  of  the  device  was  stopped  at  2.05  P.M. 

After  the  tanks  were  filled  the  blow-off 
pipes  at  the  bottom  of  the  tanks  were  opened 
for  a  few  seconds  every  fifteen  minutes,  to  re 
move  suspended  matters  which  had  settled  to 
the  bottom.  Of  the  630  cubic  feet  of  river 
water  w.hich  were  applied  to  the  device  from 
10.05  A-M-  to  2-°5  P-M.,  20  cubic  feet  were  dis 
posed  of  in  this  manner;  484  cubic  feet  passed 
through  the  tanks;  and  the  remaining  126 
cubic  feet  were  retained  in  the  tanks  and  the 
piping  system. 

During  the  operation  of  the  device  the 
voltage  and  amperage  of  the  main  circuit 
averaged  210  and  29,  respectively.  The 
voltage  on  the  electrodes  was  52. 

An  opportunity  to  obtain  adequate  obser 
vations  on  the  amount  of  metallic  aluminum 
used  was  not  afforded.  However,  taking  the 
results  of  later  experiments  as  a  basis,  it  is 
estimated  that  the  amount  of  metallic  alu 
minum  converted  electrolytically  into  alu 
minum  hydrate  averaged  about  0.15  grain  per 
gallon  of  applied  water.  The  amount  of  elec 
tric  current  was  .0129  ampere-hours  per  gal 
lon  up  to  12.05  P.M.,  and  .0497  amperejhours 
per  gallon  after  that  time.  The  corresponding 
amounts  of  electric  power  were  152  and  583 
electric  H.P.  per  million  gallons  of  water  per 
24  hours,  respectively. 

After  the  operation  of  this  device  was 
stopped  at  2.05  P.M.,  the  filter  was  washed. 
River  water  without  previous  treatment  was 
then  allowed  to  flow  through- it  for  thirty-five 


DEVICES   OPERATED    BY    THE  HARRIS  COMPANY  IN  JULY. 


minutes  (2.30-3.05  P.M.)  at  a  maximum  rate 
of  ab'out  30  million  gallons  per  acre  per  24 
hours. 

Samples  of  water  before  and  after  treatment 
by  this  device  were  collected  and  analyzed 
with  the  results  indicated  in  table  opposite. 

It  will  be  noted  in  connection  with  the 
above  results  that  the  number  of  bacteria  in 
the  water  decreased  in  passage  through  the 
tanks,  but  increased  after  filtration.  The  ex 
planation  of  this  is  that  the  filter  was  not  op 
erated  long  enough  to  wash  out  the  bacteria 
originally  contained  in  the  sand. 

In  the  next  table  are  presented  the  results 
of  analyses  of  chemical  samples  on  this  date. 

Sample  Xo.  744  was  collected  from  the 
river  water  at  9.30  A.M. 

Samples  Xos.  745  and  747  were  collected 
at  11.55  A.M.  and  2.00  P.M.,  respectively,  from 
the  water  as  it  left  the  outlet  of  the  last  tank. 

Samples  Xos.  746  and  748  were  collected 
at  11.55  A-M-  anfl  2-°°  I'.M.,  respectively,  from 
the  water  after  it  passed  through  all  the  tanks 
and  through  the  filter. 


BACTERIAL  RESULTS— 

DEVICE  N 

o.  3. 

Source  of  Sample. 

Hour  of 

Bacteria 
per  Cubic 

600 

Treated  water  from  outlet  of  last 

Treated  wa  e    after  filtration.  .  .  . 
Treated  wa  e    from  outlet  of  last 
tank  

12.00  " 

7  100 

Treated  wa  e    after  filtration.  .  .  . 
Treated  wa  e     from  outlet  of  last 

12.05     " 

9  loo 

Treated  wa  e    after  filtration.  .  .  . 
Treated  wa  e    from  outlet  of  last 
tank  

2.OO      " 

13000 

Treated  water  after  filtration  .... 

2.O5      " 

8  400 

River  water  after  filtration  with 
out  preliminary  treatment  
Treated  water  from  outlet  of  last 
tank  (12.00  M.)    after  5   hours' 

3.04      " 

251 

Treated  water  from  outlet  of  last 
tank   (2.00   P.M.)  after  3  hours' 

Sample  Xo.  752  was  collected  at  3.04  P.M. 
and  represents  river  water  after  filtration 
without  preliminary  treatment  in  the  tanks. 


CHEMICAL    RESULTS— DEVICE    No.    3. 
Analyses    of    Samples    Described    Above. 

(Parts  per  Million.) 


Collected 

Nitrogen 

Residue  on 

Fixed  Residue 

. 

after  Ignition. 

- 

<;u 

C 

Ammonia 

. 

• 

5. 

g 
-- 
7, 

Date. 

U 

S3 

M  ~ 

si 

u 

•a 

•s 

•s 

-a 

•a 

fr 

•a 

•a 

•a 

1896. 

8.3 

u 

& 

_• 

•o 

> 

V 

Z 

z 

•c 

_: 

5 

•3 

_• 

£ 

•5 

-^ 

•3 

- 

g 

•3 

£• 

£ 

i| 

.iS 

£ 

^ 

g 

n 

% 

- 

* 

'£. 

^ 

en 

§ 

</> 

(" 

u 

c 

H 

a 

o 

H 

•yi 

a 

H 

<fi 

a 

< 

a 

~ 

744    July    8 

9.30  A.M. 

25-7 

.19 

8.71-504 

.406 

.098 

.038 

.OOI 

-5 

4.0 

751 

637 

116 

668 

594 

74 

6O.3 

o.o 

33-30 

745                8 

11.55      " 

.10 

6.3-352 

.264  .oSS 

.062 

.004 

•5 

4.1 

496 

387 

109 

414 

71 

57-6 

o.o 

29.  10 

74''                8      11.55     " 

•  13 

0.8 

.082  .OOO 

.082 

.060 

.004 

•4 

4.0 

107 

0 

107 

66 

0 

66 

57-9 

o.o 

.07 

747 

8          2.0O  P.M. 

.07 

I  .2 

.128  .036 

.092 

.146.  004 

-4 

4.0 

172 

69 

103 

M4 

69 

65 

59-0 

0.6 

4.  16 

748 

8        2.00     " 

.08 

O.g 

.092 

.000 

.092 

.098  .004 

•4 

2.5 

98        o 

98 

66 

0 

66 

59-0 

o.o 

.05 

758 

8        3.04     " 

.!   - 

1-9 

.178 

.030^007 

•4 

4.0 

127 

IOI 

6o.O 

0.0 

9.20 

DEVICE  No.  4. 

The  fourth  device  presented  for  official  in 
spection  was  operated  continuously  from 
9.50  A.M.  to  3.25  P.M.  July  23,  and  from  6.30 
P.M.  July  23,  to  9.00  A.M.  July  24.  It  was 
intended  to  operate  this  device  continuously 
up  to  August  i ,  but  the  Harris  Company  de 
cided  to  make  a  further  modification  after  the 
operation  as  above  noted.  This  device  com 
prised  all  of  the  seven  closed  vessels  which 
had  been  used  before,  and  the  small  sand  fil 


ter.  The  first  small  porcelain-lined  tank 
alone  contained  electrodes  of  metallic  alu 
minum,  the  active  area  (anode  surface)  of 
which  was  about  2300  square  inches.  The 
set  of  magnets  in  this  tank  was  also  used.  On 
top  of  this  tank  was  set  the  2O-inch  stand 
pipe.  The  cover  of  the  tank  and  bottom  of 
the  stand  pipe  were  removed,  as  were  also  the 
tin  cones  in  the  pipe.  Water  to  be  treated 
entered  at  the  bottom  of  the  small  ta^nk, 
and  passed  up  through  the  stand  pipe, 
from  the  top  of  which  it  passed  to  and 


286 


WATER    PURIFICATION   AT  LOUISVILLE. 


through  the  series  of  two  small  tanks, 
and  three  large  ones,  for  the  purpose  of 
sedimentation.  The  records  of  the  operation 
of  this  device  are  presented  in  the  next  tab.es. 
For  convenience  in  presentation,  two  tables 
are  given,  the  first  giving  the  record  of  the 
device  exclusive  of  the  sand  filter,  and  the 
second,  the  records  of  operation  of  the  filter. 
Following  these  two  tables  are  presented  the 
results  of  analyses  of  samples  of  river  wa'er 
before  and  after  treatment  by  this  device. 

Alinnin:  in  Used. — Satisfactory  observations 
of  the  amount  of  metallic  aluminum  used  in 
the  treatment  of  the  water  were  not  obtained. 
The  river  water  was  very  muddy  at  this  time, 
and  examination  of  the  porcelain-lined  tank 
at  the  close  of  the  runs  showed  that  it  was 
filled  wi'h  a  very  thick  deposit  of  mud,  which 
had  subsided  during  the  passage  of  the  water 
through  this  tank  and  the  stand  pipe  placed 
on  the  top  of  it.  Another  observation  of  im 
portance  was  that,  at  the  bottom  of  the  porce 
lain-lined  tank,  there  was  found  a  large  num 


ber  of  scales  of  aluminum  oxide,  which  had 
been  formed  on  and  removed  from  the  metal 
lic  e'ectrocles  by  the  action  of  the  electric  cur 
rent. 

RECORDS  OF  OPERATION— DEVICE  No.  4. 


Number  of  Run  .... 

1 

2 

July  23,  9.50  A.M. 

Jul  v  23,  6.  20  P.M. 

Ended  

"       23,    3.25    P.M. 

'  '      24,  9.00  A.M. 

Period  of  service.  .  . 

5  hrs.  35  min. 

14  hrs.  30  min. 

Period  of  tilling  

o     "     35     " 

o     "     15     " 

Cubic  feet  of   water 

t  recited  * 

2  275                                   4  464 

Cubic  feet   of  water 

O                                               o 

Average       rate      of 

treatment 

Cubic  feet  per  min. 

6.77 

5-35 

Gallons  per  24  hrs.. 

72  goo                        57  600 

Average    voltage 

(entire  system).  .  . 

206 

214 

Average    amperage 

(entire  system).  .  . 

29.6 

26.0 

Average    electric 

ampere  hours  per 

gallonf  

.0098                          .0108 

A  v  e  rage    electric 

ii.  i'.  per  mil.  gals. 

per  24  hoursf.  .  .  . 

i  i  .• 

129 

RECORDS    OF    OPERATION    OF   THE    FILTER— DEVICE    No.    4. 


Number  of   Run 

1 

2 

3 

July  23,  9.50  A.M. 

"       23,   2.OO  P.M. 

5  hours  10  minutes. 

4       "       53 
17 
45.6 

7-5 

O.I2 

ITS 

July  23,  2.00  P.M. 
"     24,  2.50  A.M. 
9  hours  50  minutes. 
9     '•       30 
20           " 
87.8 
10.2 

0.15 
22 

July  24,  2.50  A.M. 
"     24,  9.00     " 

6  hours  10  minutes. 

Ended  

Period  of  operation  

67.8 

Average  rate  : 

0.18 
27 

Million  gallons  per  acre  per  24  hours  

RESULTS    OF    BACTERIAL   ANALYSES   OF   SAM 
PLES    COLLECTED  JULY    23,   12.00   M.—  DEVICE 
No.   4. 

Source  ofSa-Me. 

!       Bacteria  per 
Cubic  Centimeter. 

Treated  water  from  outlet  of  stand  pipe. 
Treated  water  from  outlet  of  last  tank. 
Treated  water  after  filtration  

23  200 
29  500 

4  :>"" 

Samples  of  water  before  and  after  treatment 
by  this  device  were  collected  and  analyzed  with 
the  results  presented  beyond.  Of  the  chemi 
cal  samples,  No.  763  was  collected  from  the 


river  water  before  treatment,  No.  768  was  col 
lected  from  the  water  after  it  had  passed 
through  the  first  small  tank  and  stand  pipe 
extension  thereof,  No.  769  was  taken  from 
the  water  after  it  had  passed  through  the  en 
tire  system  of  tanks,  just  before  it  was  turned 
into  the  filter,  and  No.  779  was  taken  from 
the  effluent  from  the  sand  filter. 

After  the  run  ending  July  24,  9.00  A.M.,  the 
stand  pipe  was  removed  from  the  top  of  the 
porcelain-lined  tank,  and  p'aced  on  the  floor 
again,  owing  to  the  complications  in  the 
electrolytic  cell  arising  from  the  sedimenta 
tion  which  took  place  when  in  the  first-men 
tioned  position.  The  remaining  operations 
are  described  as  those  of  Device  No.  5. 


DEVICES  OPERATED  BY    THE  HARRIS  COMPANY  IN  JULY. 


287 


CHEMICAL    RESULTS— DEVICE    No.    4. 
Analyses    of    Samples    Described    Above. 

(Parts  per  Million.) 


Z    i      Date. 

'    •'  • 


763 

768 
769 

::• 


July  23    9-30A.M 

"       23  12. OO  M. 
"       23  12. OO    " 

"       23JI2.00    " 


25.1   .37,24 
•    -23  24-5 
.   .23J24.0 

•1-331  3-7 


1.360  1.228  .132  .056 

1.280  1. 168  . 112  .026 

1.360,1 .1541 .  206^.080 

.2o6|. 1...  .[.038 


DEVICE  No.  5. 


The  fifth  and  last  device  was  presented  for 
official  inspection  on  July  27.  Five  runs  were 
made  from  July  27  to  August  i,  the  device 
being  operated  day  and  night  so  far  as  was 
feasible.  In  this  device,  as  in  the  preceding, 
all  seven  of  the  closed  vessels  were  used  as 
well  as  the  filter.  In  all  of  the  three  small 
tanks  were  sets  of  aluminum  electrodes  and 
the  magnets  on  these  tanks  were  also  used. 
The  electrode  manifold  in  the  first  tank  was 
somewhat  larger  than  in  the  second  and  third, 
the  current  (circuits  in  parallel)  dividing  as 
follows:  Electrodes  Number  i,  7.6  amperes; 
electrodes  Number  2,  5.8  amperes;  elec 
trodes  Number  3,  6.0  amperes.  The  total 
active  area  of  the  electrodes  (anode  surface) 
was  about  4000  square  inches. 

The  river  water  entered  the  first  small  tank 
at  the  bottom,  passed  through  it  and  thence 
upward  through  the  stand  pipe.  This  pipe 
was  set  on  the  ground  as  when  first  used,  the 


top  of  the  small  tank  and  the  bottom  of  the 
pipe  being  closed.  The  tin  cones  were  used 
in  this  pipe  as  in  the  third  device,  and  piping 
was  provided  to  flush  out  the  sediment  at  the 
base  of  the  cones  and  the  bottom  of  the  pipe. 
From  the  stand  pipe  the  water  passed  suc 
cessively  through  the  second  and  third  small 
tanks,  thence  through  the  three  large  tanks 
(used  as  settling  chambers)  and  finally  a  por 
tion  of  it  passed  through  the  filter.  From  July 
30,  5.50  P.M.,  to  July  31,  4.00  P.M.,  the  water 
filtered  was  taken  from  the  third  small  tank, 
instead  of  from  the  third  large  tank  which 
was  the  last  one  of  the  series. 

The  records  of  operation  of  this  device  and 
the  results  accomplished  therewith  are  pre 
sented  in  the  following  tables.  As  before, 
the  records  of  operation  of  the  device  exclu 
sive  of  the  filter,  and  of  the  filter  itself,  are 
presented  separately.  Following  these  tables 
are  presented  observations  on  the  amount  of 
aluminum  used  and  the  efficiency  of  the  elec 
tric  generating  plant. 


RECORDS   OF   OPERATION— DEVICE    No.  5. 
Records   of  Operation   of   Device   Exclusive  of   Filter. 


1 

2 

3 

4 

5 

Began  j 

July  27, 

July  28, 

July  29, 

July  30, 

July  31, 

Ended  j 

7-47  P.M. 

July  28, 

J.20  P.M. 

July  29, 

12.45  r-M- 
July  30, 

5.30  P.M 

July  31, 

Aug.  i. 

9.OO  A.M. 

6.00  A.M. 

g.OO  A.M. 

i8h.  3701. 

9  -13  A.M. 

Period  of  filling,                                "        .                               ... 

Cubic  feet  of  water  wasted  ... 

176 

Average  rate  of  treatment.      Cubic  feet  per  minute  

3.28 

I.I? 

I.I5 

I  .20 
12  qoo 

4.68 
50  400 

198 

182 

23  6 

28.8 

29.  1 

31  .  1 

Average  electric  horse-power  per  million  callous  per  24  hours  f.  . 

186 

605 

61? 

601 

150 

'  After  syste 


•itchboard  readings  of  entii 


WATER  PURIFICATION  AT  LOUISVILLE. 


Records  of  Operation   of   Filter. 


1 

Average  Rate. 

hos 

Hours  and  Minutes. 

Cubic  Feet. 

JiS 

Began. 

Ended. 

Cubic   Ft. 

Gallons 

per  Min. 

per  Acre 

i 

July  27,     7.47  P.M. 

July  27    11.18  P.M. 

4h.   iSn  . 

4!].  05111. 

"    13111. 

21  .O 

3-3 

O.  II 

16 

2 

27,  ii.  18     " 

28      4.30A.M. 

5h.  I2n  . 

4h.  57m. 

15111. 

1Q.6 

7-3 

0.07 

II 

3 

28,    4.30A.M. 

28      5.50     " 

ih.  2om. 

ih.  oom. 

2Orn. 

6.0 

17-3 

0.18 

27 

4 

23,     5.50    " 

28      8.00    " 

2h.  32n  . 

2h.  15111. 

lym. 

20.2 

12.  I 

0.15 

22 

28        8  22      " 

28 

6 

29,    12.25   l'-M. 

30        5.50  P.M. 

2oh.  5811  . 

20h.  38111. 

20111. 

255-8 

10.5 

0.21 

3' 

7 

30,      5-5"      " 

30    8.40  •• 

2h.  som. 

2h.  40111. 

loin. 

20.  O 

IO.O 

O.  12 

18 

8 

30,      8.40      " 

31         1.  25  A.M. 

4h.  45tn. 

4(1.  33111. 

12m 

35-" 

12.0 

0.13 

19 

9 

31,       1.25  A.M. 

31       6.20     " 

3h.  5511  . 

3".  45"'. 

lorn. 

2S.O 

13-5 

O.  II 

1  6 

10 

31,       5-20      " 

31        3.50  P.M. 

6h.  54m. 

61,  .  47111. 

oym. 

54-5 

I4.8 

0.13 

'9 

II 

31,      3.^0  I'.M. 

31        4.00      " 

oh.  3211  . 

oh.  2om. 

I2m. 

4-4 

13-3 

O.22 

33 

12 

3",     4-00     " 

Aug.      I      9.43  A.M. 

I7h.  I3in. 

202.9 

0.20 

30 

During  runs  numbers  7  to  n,  inclusive,  the  water  to  be  filtered  was  taken  from  the  third  small  porcelain-lined  tank. 

During  all  the  other  runs  it  was  taken  from  the  last  large  tank. 

Results  of  Analyses — Device  No.  5. 

In  the  following  tables  are  presented  re 
sults  of  frequent  analyses  of  the  water  before 
and  after  treatment  by  this  device.  Samples 
were  collected  from  the  water  before  treat 
ment,  after  it  had  passed  through  the  first 
tank,  after  it  left  the  last  tank,  and  after  it 
had  passed  through  the  filter. 

The  first  table  shows  the  results  of  the  bac 
terial  analyses  of  the  river  water  before  treat 
ment,  during  the  periods  when  this  device  was 
in  operation. 

In  the  second  table  are  given  the  results  of 


bacterial  analyses  of  the  treated  water  after  it 
had  passed  through  the  first  tank. 

The  third  and  fourth  tables  contain  the  re 
sults  of  bacterial  analyses  of  the  treated  water 
from  t'he  last  tank  and  of  the  effluent  from  the 
filter,  respectively. 

Following  these  are  tables  containing  the 
results  of  the  corresponding  chemical  anal 
yses,  the  time  and  place  of  collection  being 
given  by  reference  to  the  corresponding  bac 
terial  samples.  When  two  or  more  bacterial 
numbers  are  given  it  is  to  be  understood  that 
portions  collected  at  the  same  time  and  place 
as  these  bacterial  samples  were  mixed  and  the 
analvsis  made  of  the  mixture. 


BACTERIAL  RESULTS— RIVER  WATER. 


Number 

Colle 

cted. 

Bacteria  per  Cubic 

Sample. 

Date. 

1896. 

Hour. 

Centimeter. 

4726 

July  27 

g.30A.M. 

16  ooo 

473° 

27 

5.00  P.M. 

19  600 

4741 

27 

9.00     " 

14  400 

4745 

28 

3.00A.M. 

18  500 

4750 

28 

9-30      " 

24  500 

4796 

28 

6.OO  P.M. 

12  400 

4800 

28 

12.00      " 

8  600 

4804 

29 

6.0O  A.M. 

10  700 

4812 
4861 

29 

9.30     " 
5  OO  P.M. 

9500 

4866 

29 

30 

9.30  A.M. 

17300 

4871 

30 

5.OO  P.M. 

6  800 

4878 

3i 

9.30  A.M. 

6  800 

4881 

3i 

10.45      " 

7900 

4891 

3i 

3-35  P.M. 

5  800 

4898 

3i 

4.30     " 

8  600 

4899 

3i 

4-30      " 

9  600 

BACTERIAL  RESULTS— DEVICE  No.  5. 
Effluent  from  first  tank. 


Collected. 

Number 

Bacteria 

Sample. 

Date. 

1896. 

Hour. 

Rate. 

per  Cubic 
Centimeter. 

4738 

July  27 

9.00  P 

M. 

2.6 

12  7OO 

4742 

28 

3-00  A 

M. 

2.5 

12  900 

4747 

28 

g.OO 

* 

4-4 

15  ooo 

4797 

28 

6.OO  P 

M. 

.0 

2  900 

4801 

28 

12.  OO 

* 

.0 

3900 

4805 

29 

6.00  A 

M. 

.0 

5700 

4856 

29 

3.05  P 

M. 

•3 

5  800 

48663 

3" 

g.OO  A 

M. 

.2 

5  800 

4872   ;          30 

5.30  P 

M.               .0 

i  500 

4875      ;                  31 

8.OO  A 

M.               .  I 

3  600 

4879 

31 

IO.2O 

"                   .2 

5  600 

4884 

31 

12.05  P 

.M.              .2 

2  800 

4894 

31 

4.IO 

4.2 

IO  100 

4900 

31 

5.0O 

3.8 

4  600 

4904 

Aug.     i 

9.00A.M.     .       4-0 

2  OOO 

1  Rate  of  treatment  in  cubic  feet  per 


DEVICES   OPERATED   BY    THE   HARRIS   COMPANY  IN  JULY. 


289 


BACTERIAL  RESULTS-DEVICE  No.  5. 
Effluent  from  last  tank. 


Number 
Sample. 

Collected. 

Rate.* 

Bacteria 
per  Cubic 
Centimeter. 

Date. 

1896. 

Hou, 

473° 

July  27 

g.OO  P.M. 

2.6 

I  800 

4743 

"     28 

3.OO  A.M. 

2.5 

5  300 

4748 

"     28 

9.00      " 

4.4             15  ooo 

4798 

"     28 

6.OO  P.M. 

i-o                 215 

4802 

••     28 

12.  OO      " 

10                 192 

4806 

"     29 

6.00A.M. 

i.o                 252 

4857 

•     29 

3.05   P.M. 

i  .  3                 700 

48&7a 

"     30 

g.OO  A.M. 

1.2 

900 

4876 

"     30 

g.OO      " 

1.2 

900 

48833 

"     3' 

11.40      " 

I    2 

310 

4885 

11     31 

I2.O5  P-M. 

1.2 

25O 

4895 

"     31 

4.10      " 

4-2 

7  800 

4901 

"     31 

5.00      " 

3-8 

2  OOO 

4905 

Aug.     I 

g.OO  A.M. 

4.0 

3  5°o 

ubic  feet  pe 


BACTERIAL   RESULTS—  DEVICE    No.  5. 

Effluent  from  Filter. 

Collected. 

Number 

Bacteria  per 

of 
Sample.              Date 

Hour. 

Rate.* 

Cubic 

1896. 

474° 

July    27 

g.OO  P.M. 

0.26 

132 

4744 

28 

3.OO  A.M. 

o  .  09 

So  • 

4749 

28 

9.00      " 

0.  II 

I  800 

4799 

"        28 

6.00    P.M. 

O.2O 

262 

4803 

28 

12  00       " 

0.20 

399 

4807 

"        29 

G.OO  A.M. 

0.2O 

188 

4858 

29 

3.05    P.M. 

0.25 

171 

4863 

29 

5.12       " 

O.24 

700 

4868a 

30 

g.OO  A.M. 

o.  14 

435 

4873 

30 

5.30  P.M. 

0.14 

130 

4877 

31 

S.OO  A.M. 

0.15 

173 

4880 

31 

10.20      " 

0.13 

300 

4886 

31 

12.05    P.M. 

0.13 

505 

4896 

"        31 

4.10       " 

O.  21 

I  500 

4902 

31 

5-00       " 

0.24 

700 

4906 

Aug.     I 

9.00    \.  M. 

0.23 

700 

»  Cubic  feet  per  minute. 

CHEMICAL    RESULTS— DEVICE   No. 

(Parts  per  Million.) 


< 

•o 

Nitrogen 

Residue  on 

Fixed  Residue 

*• 

^ 

t 

e 

Evaporation. 

after  Ignition. 

1 

a 

Date  of               Ku 
Collection.             S. 

G 

c 

asAlbuminoid 

. 

3 

•o 

jj 

'"•? 

h 

I 

u 

o 

S 
t- 

If 

Q| 

^  e 

"  E 

< 

•z. 

X 

.-. 

h 

a. 

3 

i 

h 

c 
a 

'£ 

c 

M 

Q 

i 

781' 

July  27 

•  27 

18.8 

I.I20 

I  .OO2 

.118 

.124 

.019 

.76.5 

1496 

1387 

109 

1356 

1286 

70 

55-1 

0.0 

70.80 

782' 

27-28 

•3i 

13.2 

.740 

.622 

.118 

.092 

.018 

.6 

6.5    1061 

952   109 

950 

880 

70 

55.2 

o.o 

20.00 

783' 

787* 

"      27-28 
"      28-29 

•  30 

3-5 

.I58 

.040 

.118 

.044  .on 

.6 

g 

6.5 

166 

57 

[09 

124 

54  70 

51.0 

0.0 

2.OO 

788' 
789' 

"      28-29 
"      28-29 

.10 

.12 

2-4 
2.1 

.102 
.080 

.012 

.090 

.216 
.144 

.033 

.  IOO 

i: 

6.0 
4-0 

"5 

87 

26    89 

94 
62 

31 

63 

46.8 
49-0 

o.o 
o.o 

.70 

.  12 

794' 

"      29-30 

.11 

ii.  8     .630 

•530 

.  IOO  .  2O2 

.023 

.8 

T.I 

926 

826 

IOO 

841 

774 

67  56.0 

0.0 

34.50 

795" 
796" 

"      29-30 

.11 

3.0     .150 

•  050 

.100  .194 

.032 

•9 

3.0 

194 

94 

IOO 

163 

96 

67,52.2 

0.0 

6.50 

7991" 

31 

13 

10.2      .680 

.5881.092  .248 

.012 

•  7 

628 

536 

92 

560 

493 

67 

52.6 

o.o 

28.70 

31 

.07 

2.0      .088 

.ooo|.o88 

.  140 

•333 

.6 

1.6 

92 

0 

93 

68 

o 

(,- 

53-J 

0.0 

.05 

31 

•13 

2.3     .no 

.018 

.092 

.208 

.020 

.6 

!•  i 

130 

3S 

IOI 

34 

''7 

51-1 

o.o 

.70 

'     31,   Aug.  i 

..  .27  11.3    .540 

.418 

.  122  .042  .006 

.8 

4.0 

699 

576 

123 

634 

54490  62.0 

o.o 

25.30 

805" 

3'i         'I 

.27  ii.  9     .510 

-.388 

.  122  .040  .006 

•  8 

1-7 

6^8 

535 

123 

583 

4939043.0 

0.0 

24.50 

'     3'p        "     i 

.27    4.3     .198 

.076 

.122  .026J.OP4 

.s 

;  - 

204 

-i    123 

163 

73  90  50.0 

o.o 

9.00 

•4799,4803,4807.    '  4856.  4806,1.    "4857,4867,1.    '4858.4868,1.     '»  4879.    "4080.     "4883,1.     i>  4900,  4904.    '<  4901,  4905.    "4902,4906. 

SUMMARY  OF  ANALYTICAL  RESULTS — 
DEVICE  No.   5. 

The  degree  of  purification  accomplished  by 
the  fifth  device,  at  different  points  in  the  pas 
sage  of  the  water  through  it,  is  indicated  by 
the  following  tables.  The  removal  of  organic 
matter  as  indicated  by  the  nitrogen  in  the 
form  of  albuminoid  ammonia  and  oxygen 
consumed  is  first  presented.  Following  this 
is  given  a  summary  of  the  bacterial  analyses 
of  the  water  at  different  points  on  its  passage 
through  the  device. 


PERCENTAGE  REMOVAL  OF  ORGANIC  MATTER 
FROM  THE  RIVER  WATER  AT  DIFFERENT 
POINTS  ON  ITS  PASSAGE  THROUGH  THE 
DEVICE. 

Percentage  Removal  of  Nitrogen  as  Albuminoid 
Ammonia. 


Point  of  Collection  of  Sample. 

First  Tank. 

Last  Tank. 

Filter. 

July 

28 

O 

34 

93 

29 

63 

88 

91 

30 

48 

88 

<H 

" 

3i 

0 

77 

Si 

Aug. 

i 

o 

o                       58 

Percentage    Removal   of  Oxygen   Consumed. 

July  28  o 

"     29  64 


"     3« 

"     31 

Aug.     i 


290 


WATER   PURIFICATION  AT  LOUISVILLE. 


SUMMARY  OF  BACTERIAL  RESULTS. 

BACTERIA  PER  CUBIC  CENTIMETER  IN  THE 
RIVER  WATER  BEFORE  TREATMENT  AND  AI 
DIFFERENT  POINTS  ON  ITS  PASSAGE  TH  ROUGH 
THE  DEVICE. 


Date.  1896. 

Ju  y  27 

Ji 

Iy28 

uly  28 

July  28 

July 

Julyag 

July2, 

Hour... 
River  
First  Tank 
Last   Tank 
Filter...    . 

V 

12 

I 

M 

•j 

400 
7OO 
800 
132 

iS  500  24  500 
1  2  900   1  5  ooo 
5  300  1  5  ooo 
So     i  Soo 

12  400 
2  900 
215 

262 

8  600 
3  900 
192 
399 

10  700 
5  7°° 
252 

188 

9500 
5  Soo 
700 
171 

Date. 

1896. 

July  30 

July3o 

Julys' 

Julys 

•Julys 

:  July 

3 

Julys- 

Auif.  ' 

Hour.. 
River.. 

First 

9  A 
17 

.M. 

3OO 

5  P.M. 

6800 

SA.M 
6  Soo 

I  O  A.  .1 

6  So 

.  12    M 

3  7  900 

4   P.M.  5  P.M. 
9  100  9  100 

(JA.M. 

6  Suo 

tank. 
Last 

5  Soo 

1  500 

3  600 

5  60 

3    2  SOC 

10  100  4  600 

2  000 

tank. 
Filter.  . 

900 
435 

130 

I  200 

'73 

3 

250     7  Soo  2  ooo 

31       505:      I   500,       700 

3  500 
70  J 

AVERAGE 

BACTERIA 

IN 

RIVER     WATER 

AND 

AT 

DIFFERENT      POINTS      IN      ITS 

PASSAGE 

THROUGH 

THE 

DEVICE, 

AND    THE 

AVERAGE 

PERCENTAGE 

REMOVAL 

AT    T 
River. 

HESE 

POINTS. 

First 
Tank. 

6  320 
40 

TLant!    Fi'f. 

Average 
Average 

bacter 
percen 

a  per  c.  c  
tage  removal  

II  300 

3  ooo      500 
76        96 

From  July  27,  7.47  P.M.,  to  July  30,  9.00 
A.M.,  37  440  gallons  of  water  were  treated 
and  the  weight  of  the  aluminum  electrodes 
decreased  18  620  grains,  equal  to  0.5  grain 
per  gallon. 

From  July  30,  9.00  A.M.,  to  July  31.  12.07 
P.M.,  9465  gallons  of  water  were  treated  and 
the  weight  of  the  aluminum  electrodes  de 
creased  7490  grains,  equal  to  0.78  grain  per 
gallon. 

From  July  31.  12.07  i'-M->  to  Aug.  i,  9.43 
A.M.,  34  500  gallons  of  water  were  treated 
but  there  was  no  reduction  in  weight  of  elec 
trodes,  owing  to  a  failure  in  the  electrical  con 
nections. 

It  is  to  be  stated  that,  of  the  amount  of  alu 
minum  noted  above,  a  considerable  portion 
passed  into  the  oxide  state;  scaled  off  the 
electrodes,  fell  to  the  bottom  of  the  tanks  and 
was  of  no  aid  in  the  purification  of  the  water. 
Further,  it  was  impracticable,  under  the  ex 
isting  circumstances,  to  determine  how  much 
of  the  aluminum  which  was  removed  from 
the  electrodes  by  the  electric  treatment  was 


actually    utilized    in    the    purification    of    the 
water. 


Arrangements  were  made  to  study  this 
point,  but  after  some  work  had  been  done  it 
was  seen  that  no  results  of  practical  value 
were  being  obtained,  because  it  was  not 
known  how  much  aluminum  in  the  form  of 
available  hydrate  had  actually  been  added  to 
any  sample  of  water  for  analysis. 

This  work  was  stopped  and  taken  up  under 
more  favorable  conditions  after  Aug.  i  and 
is  described  in  the  next  chapter. 

Efficiency  of  the  Electric  (Generating  Plant  of  the 

Harris  Magneto-electric  ll'aicr 

Purification  S \stcin. 

Three  tests  were  made  of  the  relation  be 
tween  the  steam  and  electrical  power,  show 
ing  the  average  combined  efficiency  of  the 
generating  plant  to  be  21.8  per  cent. 

STATUS   OF  THE   SITUATION   ON   AUGUST    i, 
WITH  REGARD  TO  THE  MAGNETO-ELEC 
TRIC  SYSTEM  AND  DEVICE. 

The  more  important  features  of  the  situa 
tion  on  Aug.  i,  when  the  investigations  upon 
the  other  systems  of  purification  were 
brought  to  a  close,  may  be  briefly  summa 
rized  as  follows: 

1.  The  original  system  was  a  complete  fail 
ure  at  the  time  of  official  examination;    and, 
practically  speaking,  it  was  abandoned  there 
after  by  the  Harris  Company. 

2.  It  is  possible  to  purify  the  Ohio  River 
water  to  a  greater  or  less  degree  by  the  appli- 

:ation  of  aluminum  hydrate  prepared  electro- 
lytically  from  metallic  aluminum.  With  other 
ivaters  purification  in  this  or  a  similar  manner 
had  been  previously  claimed  by  other  per- 

ions. 

3.  The  available  data,  so  far  as  they  went, 
indicated  that  the  direct  effect  of  the  electric 
action  and  the  magnetic  action  was  of  little 

r  no  practical  value. 

4.  It  is  possible  to  purify  the  Ohio  River 


DEVICES   OPERATED   BY    THE  HARRIS  COMPANY  IN  JULY. 


291 


water  to  a  satisfactory  degree  with  electroly- 
tically  formed  aluminum  hydrate  by  the  em 
ployment  of  subsequent  sedimentation  and 
filtration.  Further,  no  lime  in  the  river  water 
is  required  with  this  process,  and  there  is  no 
increase  in  the  corroding  and  incrusting  con 
stituents  of  the  filtered  water. 

5.  The  available  data,  so  far  as  they  went, 
indicated  that  the  manner  of  purification  last 
stated  would  be  costly  to  an  excessive  and  un 
reasonable  .degree  if  applied  to  the  water 
supply  of  a  large  city.  It  appeared,  further, 
that  in  continuous  service  it  might  allow  per 
iods  of  marked  irregularity  in  efficiency. 

6.  Viewed  from  a  practical  point,  the  data 
which  it  was  feasible  for  the  Water  Company 
to  obtain,  under  the  existing  circumstances, 
were  very  limited  and  unsatisfactory.     This 
was  due  chiefly  to  the  poor  and  ill-advised 
construction  of  the  devices  as  they  were  as 
sembled   together,  and,   further,   to   the   fact 
that  the  total  period,  during  which  the  de 
vices  were  operated  for  official  inspection,  was 
less  than  119  hours. 

7.  The  situation  may  be  comprehensively 
described  by  the  statement  that  this  method 
of  purification  had  not  advanced  beyond  the 
experimental  stage,  where  laboratory  experi 
ments  are  best  adapted  to  show  the  practica 
bility  and  merits  of  the  method. 

From  the  above  statements  it  is  plain  that 
at  the  close  of  the  regular  investigations  the 
situation  with  regard  to  the  magneto-electric 
devices  was  quite  unsatisfactory,  from  the 


Water  Company's  point  of  view,  as  well  as 
from  thai  of  the  Harris  Company. 

The  indications  were  that  the  method  was 
not  a  commercial  success,  so  far  as  the  purifi 
cation  of  the  Ohio  River  water  is  concerned. 
But,  owing  to  the  unsatisfactory  manner  of 
the  construction  and  operation  of  the  several 
devices,  the  very  limited  evidence  was  ob 
scured  by  a  variety  of  complications;  and 
there  was  really  obtained  very  little  informa 
tion  of  positive  value. 

A  conference  was  held  at  this  time  by  the 
officers  of  the  Water  Company  to  discuss  the 
situation.  The  advisability  of  continuing  the 
investigation  with  the  makeshift  devices 
offered  for  inspection  was  out  of  question. 
The  real  problem  was  to  decide  whether  it 
would  be  wiser  for  the  interests  of  the  Water 
Company  to  dismiss  the  subject  as  it  stood,  or 
to  have  the  fundamental  principles  of  the 
method  investigated  by  the  experts  who  were 
regularly  employed  by  the  Water  Company 
at  that  time.  It  was  decided  to  pursue  the 
latter  course.  The  Chief  Chemist  and  Bac 
teriologist  was  instructed  to  retain  the  ser 
vices  of  the  assistant  analysts  for  two  or  three 
weeks  or  so.  An  arrangement  was  also  made 
with  the  Harris  Company  to  make  use  of  their 
dynamo  and  other  electrical  appliances;  and 
the  services  of  the  man  who  had  operated  the 
devices  were  also  availed  of. 

The  results  of  these  investigations  by  the 
Water  Company  are  presented  in  the  next 
chapter. 


292 


WATER  PURIFICATION  AT  LOUISVILLE. 


CHAPTER  Xii. 

INVESTIGATIONS  BY  THE  WATER  COMPANY    IN  AUGUST  INTO  THE  PRACTICABILITY  AND 
ECONOMY  OF  THE  DEVICES  OPERATED  BY  THE  HARRIS  COMPANY. 


IN  this  chapter  there  are  recorded  the  re 
sults  of  the  various  experiments,  which  were 
made  by  the  Water  Company  under  my  direc 
tion  during  August,  1896,  with  the  view  to 
learning  the  practicability  and  economy  of  the 
principles  upon  which  the  magneto-electric 
treatment  of  water  was  claimed  to  be  based. 

The  principal  points  of  importance,  to 
which  attention  was  directed,  may  be  out 
lined  as  follows: 

1.  The  direct  and  indirect  effect  of  the  ap 
plication  of  electricity  upon  the  bacteria  and 
organic  matter  in  the  Ohio  River  water. 

2.  The  direct  and  indirect  effect  of  the  ap 
plication  of  electricity  in  the  purification  of 
the  Ohio  River  water  through  the  formation 
of  aluminum  hydrate,  from  metallic  aluminum 
electrodes. 

3.  A  comparison  of  the  efficiency,  in  the 
purification    of    the    Ohio    River    water    bv 
coagulation  and  sedimentation,  of  aluminum 
hydrate  formed  electrolytically  from  the  me 
tallic    aluminum,    and    of    aluminum    hydrate 
formed  from  the  decomposition  of  sulphate 
of  alumina  by  lime. 

4.  The  effect  of  the  action  of  the  electro 
magnets  upon  the  constituents  of  the  Ohio 
River  water,  and  upon  the  rate  at  which  alu 
minum    hydrate    is    formed    from    aluminum 
electrodes. 

5.  Rate    at    which    aluminum    hydrate    is 
formed    electrolytically     from     metallic    alu 
minum. 

6.  Regularity    during    continuous    service 
of    the    rate    at    which    aluminum    hydrate    is 
formed    electrolytically     from     metallic    alu 
minum. 

7.  Amount  of  metallic  aluminum  which  is 


wasted  in  the  electrolytic  production  of  alu 
minum  hydrate. 

8.  A  comparison  of  the  cost  of  aluminum 
hydrate  formed  by  the  application  of  sulphate 
of  alumina,  and  by  the  action  of  electricity 
on  metallic  aluminum,  respectively. 

9.  Observations  on  the  amount  of  power 
which    would    be    required    to    produce    alu 
minum  hydrate  in  a  large  scale  by  means  of 
electricity. 

The  experiments  which  were  made  on  the 
several  problems  will  be  described  in  order. 

THE  DIRECT  AND  INDIRECT  EFFECT  OF  THE 
APPLICATION  OF  ELECTRICITY  UPON  THE 
BACTERIA  AND  ORGANIC  MATTER  IN 
THE  OHIO  RIVER  WATER. 

Experiment  No.   i. 

This  experiment  was  made  to  learn  the 
effect  of  a  current  of  high  voltage,  such  as 
used  in  the  "  spark  drum  "  of  the  original 
system  (Chapter  X). 

River  water  was  treated  with  an  electric 
current  of  high  voltage  for  one  hour  in  the 
porcelain-lined  "  spark  drum  "  with  the  poles 
2.56  inches  apart.  The  voltage  of  the  current 
as  it  left  the  Ruhmkorff  coil  used  could  not 
be  accurately  measured,  but  was  estimated  by 
the  representative  of  the  Harris  Company  to 
be  about  200.000.  with  an  amperage  equiva 
lent  to  a  very  small  fraction  of  one  unit.  This 
experiment  was  performed  in  duplicate.  The 
temperature  of  the  river  water  increased 
about  2°  C.  during  this  treatment  for  one 
hour.  At  the  beginning  of  the  experiments 
the  temperature  of  the  river  water  was  31°  C. 
The  average  results  of  bacterial  analyses  of  a 


INVESTIGATIONS   OF    THE  PRINCIPLES  OF   THE  HARRIS  DEVICES.      29,5 


corresponding  set  of  samples  in  the  two  e 
periments  are  as  follows: 

REMOVAL  OF  BACTERIA  IN  OHIO  RIVER  WATER 
BY  ELECTRIC  TREATMENT  IN  THE  "SPARK 
DRUM." 


Length  of 

Bacteria 

Length  of 

of  River 
Water. 

per  Cubic 
Centi 

of  River 
Water. 

per  Cubic 
Centi 

D     age       1 

Minutes. 

me  er. 

Minutes. 

meter. 

3 

23  600 

M 

3" 

1  6  goo 

38 

5 

20  500 

25 

45 

17  2OO 

37 

10 

2O  f)OO 

25 

60 

14  loo 

48 

The  carbonaceous  organic  matter  in  the 
river  water  was  reduced  by  this  treatment,  as 
indicated  by  the  "  oxygen  consumed,"  from 
9.8  to  7.9  and  7.3  parts  per  million  in  15  and 
60  minutes,  respectively.  No  effect  was  ap 
parently  produced  upon  the  nitrogenous  or 
ganic  matter  in  the  river  water. 

Experiment  No.  2. 

This  experiment  was  made  to  learn  the 
effect  of  currents  of  comparatively  high 
density,  and  to  study  the  effect  of  amount  of 
current,  it  was  performed  in  duplicate  with 
small  carbon  electrodes  using  as  high  amper 
age  and  low  voltage  as  it  was  practicable  to 
obtain  under  the  circumstances.  River  water 
was  treated  in  a  glass  jar  for  10  minutes,  when 
the  temperature  of  the  water  became  so  high 
that  it  was  necessary  to  stop  the  experiment 
in  each  case.  The  average  amperage  and 
voltage  of  the  current  in  these  experiments 
were  10.5  and  40,  respectively,  and  the  density 
of  the  current  was  about  90  amperes  per 
square  foot  of  cross-section  of  electrolyte. 
The  average  results  of  bacterial  analyses 
of  a  corresponding  set  of  samples  in  the  two 
experiments  were  as  follows: 

REMOVAL  OF  BACTERIA-  IN  OHIO  RIVER  WATER 
BY  ELECRIC  TREATMENT,  AS  ABOVE  STATED. 


Length  of  Treat 
ment  of  River 
Water.     Minutes. 

Ampere-hours 
per  Gallon. 

Bacteria  per 
Cubic 
Centimeter. 

•JuSST 

I 

5 
10 

O 

o.  23 

0.70 
I-I7 
2.33 

28  500 

22  2OO 
13  30O 

7  7"« 
2  700 

22 
53 
73 
Qi 

The  average  temperature  at   the  close  of 
the  tests  was  53°  C.,  which  was  so  high  that 
by  actual  experiment  it  was  found  to  be  the 

explanation  for  the  removal  of  70  per  cent, 
of  the  bacteria  originally  present  in  the  river 
water. 

There  was  a  noticeable  disintegration  or 
change  in  the  nitrogenous  organic  matter, 
but  there  was  practically  no  purification  by 
the  direct  application  of  electricity.  The 
change  in  carbonaceous  organic  matter  could 
not  be  determined  owing  to  the  presence  of 
carbon  from  the  electrodes. 

No  apparent  effect  directly  or  indirectly  on 
the  rate  of  sedimentation  of  the  river  water 
was  noted  after  these  electric  treatments  with 
carbon  electrodes. 

It  may  be  added  here  that  experiments  in 
1897  bore  out  this  fact  that,  directly,  the  elec 
tric  current  had  no  practical  effect  in  the 
purification  of  the  Ohio  River  water. 

THE  DIRECT  AND  INDIRECT  EFFECT  OF  THE 
APPLICATION  OF  ELECTRICITY  IN  THE 
PURIFICATION  OF  THE  OHIO  RIVER 
WATER  THROUGH  THE  FORMATION  OF 
ALUMINUM  HYDRATE  FROM  METALLIC 
ALUMINUM  ELECTRODES. 

In  this  connection  experiments  similar  to 
the  one  last  described  were  made  except  that 
metallic  aluminum  electrodes  were  used  in 
place  of  carbon  ones.  River  water  was 
treated  in  a  glass  jar  for  10  minutes  with  a 
current  having  an  average  amperage  and 
voltage  of  6.3  and  97,  respectively.  At  the 
conclusion  of  the  experiment  the  contents  of 
the  jar  were  well  mixed,  and  a  portion  re 
moved  for  analysis. 

Sedimentation  rapidly  took  place  in  the  re 
maining  portion  in  the  jar.  The  supernatant 
liquid  was  clear  and  of  a  satisfactory  quality 
with  regard  to  organic  matter  and  bacteria. 
About  0.75  gallon  was  used  in  this  experi 
ment,  and  the  amount  of  treatment  was  1.05 
ampere  hours.  Assuming  full  rate  of  decom 
position,  the  amount  of  aluminum  added  to 
the  water  was  therefore  about  n.o  grains. 

This  indirect  purification  of  the  river  water 
by  means  of  the  production  of  aluminum  hy 
drate  was  very  marked  and  will  be  more 
clearly  presented  in  the  next  section. 

For  the  purpose  of  learning  the  direct  effect 
of  this  electrical  treatment,  independent  of 
the  subsiding  action,  analyses  were  made  of 


294 


WA'IER   PURIFICATION   AT   LOUISVILLE. 


the  unsettled  portion  of  the  treated  water. 
Here  it  may  be  stated  that  analyses  of  the 
gas,  which  was  liberated  quite  rapidly  from 
the  negative  pole,  showed  ii  to  he  composed 
very  largely,  if  not  wholly,  of  hydrogen.  The 
number  of  bacteria  in  the  river  water  before 
and  after  this  treatment  were  found  to  be 
3800  and  4200  per  cubic  centimeter,  respect 
ively. 

The  results  of  chemical  analyses  of  the 
water  befc  re  and  after  treatment  without  sub 
sidence,  represented  by  samples  Nos.  807  and 
808,  respectively,  are  presented  in  the  next 
table.  It  will  be  noted  that  the  oxygen  con 
sumed  (carbonaceous  matter)  was  reduced 


from  9.7  to  8.3  parts.  With  regard  to  the 
nitrogen  as  free  ammonia  and  albuminoid 
ammonia,  the  results  show  that  a  certain 
change  was  effected  in  the  nitrogenous  or 
ganic  matter.  Liut  as  there  was  no  marked 
increase  in  nitrogen  in  the  oxidized  form  of 
nitrites  or  nitrates,  this  condition  cannot  be 
regarded  as  one  of  purification, — it  was  simply 
an  initial  step  in  that  direction. 

This  experiment,  which  was  duplicated  in 
its  most  important  parts,  leads  to  the  conclu 
sion  that  the  direct  action  of  the  electricity 
applied  to  the  river  water  by  means  of  alu 
minum  electrodes,  without  subsidence,  ef 
fected  practically  no  purification. 


RESULTS    OF    CHEMICAL   ANALYSES   OF   SAMPLES    AS    DESCRIBED    ABOVE. 
(Parts    per   Million.) 


Collected 

Nitrogen 

Residue  on 

Fixed  Residue 

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as 

« 

Kvapoiation. 

after  Ignition. 

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0.2  23.OO 

A  COMPARISON  OF  THE  EFFICIENCY,  IN  THE 
PURIFICATION  OF  THE  OHIO  RIVER 
WATER  BY  COAGULATION  AND  SEDI 
MENTATION,  OF  ALUMINUM  HYDRATE 
FORMED  ELECTROLYTICALLY  FROM  ME 
TALLIC  ALUMINUM,  AND  OF  ALUMINUM 
HYDRATE  FORMED  FROM  THE  DECOM 
POSITION  OF  SULPHATE  OF  ALUMINA  BY 
LIME. 

Preliminary  experiments  indicated  that 
aluminum  hydrate,  formed  from  the  decom 
position  of  sulphate  of  alumina,  was  some 
what  more  effective  in  the  purification  of  the 
river  water  than  was  the  case  with  the  same 
amount  of  aluminum  hydrate  when  pre 
pared  electrolytically  from  metallic  aluminum. 
The  reason  of  this  appeared  to  be  that 
the  particles  of  aluminum  hydrate  in  the 
first  instance  were  smaller  and  more  numer 
ous  than  in  the  case  where  this  compound  was 
formed  clectrolytically.  This  explanation  of 
the  observations  seemed  plausible  by  virtue  of 
the  fart  that  electrolytically  formed  aluminum 


hydrate,  being  present  in  larger  particles  at  the 
beginning,  could  produce  fewer  centers  of  co 
agulation;  and  that,  since  the  purification 
was  brought  about  by  coagulation  and  sedi 
mentation,  the  finer  particles  of  the* precipi 
tate  formed  from  sulphate  of  alumina  gave  a 
better  opportunity  for  the  cumulative,  en 
veloping  and  coagulating  action  of  the  alu 
minum  hydrate. 

Three  sets  of  carefully  prepared  experi-' 
ments  were  made  to  obtain  accurate  data 
upon  this  point,  and  to  learn  the  correctness 
of  the  theory  presented  above.  A  descrip 
tion  of  each  set  of  these  experiments  is  next 
presented,  followed  by  a  summary  of  the 
practical  results  obtained  therefrom  and  a 
record  of  the  results  of  analyses. 

Experiment  No.   T. 

On  August  1 1  three  separate  portions  of  the 
same  sample  of  river  water  were  treated,  re 
spectively,  with  0.88  grain  of  aluminum  hy 
drate  prepared  in  the  following  manner: 

In  the  first  portion  this  amount  of  alumi- 


INVESTIGATIONS   OF    THE  PRINCIPLES   OF    THE  H. 


DEVICES.      295 


num  hydrate  was  prepared  electrolytically  in 
the  water  from  metallic  aluminum. 

In  the  second  portion  the  given  amount  of 
aluminum  hydrate  was  obtained  by  adding 
a  calculated  quantity  of  sulphate  of  alumina, 
which  was  decomposed  in  the  water  by  the 
lime  and  magnesia  present  there. 

in  the  third  portion  there  was  added  the 
stated  amount  of  aluminum  hydrate  in  the 
form  of  a  gelatinous  mass,  prepared  from  suit 
able  chemicals  in  the  laboratory. 

This  amount  of  aluminum  hydrate  (1.08 
grains  per  gallon)  corresponds  to  0.31  grain 
of  metallic  aluminum  per  gallon  of  water. 

The  experiments  were  made  with  about 
2  gallons  of  water. 

At  the  conclusion  of  the  treatment  the 
water  was  well  mixed  and  allowed  to 
remain  undisturbed  for  24  hours.  Samples 
of  the  clarified  water  were  removed  by  means 
of  a  siphon  and  subjected  to  chemical  and 
bacterial  analyses  with  results  which  are  pre 
sented  beyond,  together  with  those  of  the  un 
treated  water. 

Experiment  No.  2. 

On  August  14  the  above  experiment  was 
duplicated  with  the  river  water  of  that  day, 
with  the  exception  that  the  amount  of  alu 
minum  hydrate  added  in  each  case  was  0.51 
grain  per  gallon,  equivalent  to  0.18  grain  of 
metallic  aluminum  per  gallon  of  water. 

Chemical  and  bacterial  analyses  were  made 
of  the  river  water  after  subsidence  for 
24  hours.  Determinations  were  also  made  of 
the  number  of  bacteria  and  amount  of  sus 
pended  matter  in  the  clarified  water  after 
sedimentation  for  5  and  20  hours,  respec 
tively. 

Experiment  No.  j. 

On  August  18  the  above  experiment  was 
duplicated,  for  the  most  part,  with  the  river 
water  of  that  day.  The  amount  of  aluminum 
hydrate,  and  its  equivalent  of  metallic  alu 
minum,  were  0.14  and  0.05  grain  per  gallon, 
respectively. 

In  this  experiment  an  important  modifica 
tion  in  the  manner  of  application  of  alumi 
num  hydrate  to  the  third  portion  of  the  water 
was  made,  with  the  view  to  demonstrating 
more  positively  the  accuracy  of  the  above 


stated  theory  in  explanation  of  the  varying 
results  obtained.  Instead  of  adding  to  the 
third  portion  the  stated  amount  of  aluminum 
hydrate  in  the  form  of  a  gelatinous  mass,  the 
following  procedure  was  adopted: 

The  calculated  amount  of  sulphate  of  alu 
mina  (the  same  as  was  added  to  the  second 
portion)  was  added  to  10  per  cent  of  the  pre 
scribed  volume  of  water.  After  standing 
15  minutes,  during  which  the  sulphate  of  alu 
mina  was  decomposed  by  the  lime  and  mag 
nesia  into  aluminum  hydrate,  the  remaining 
quantity  of  untreated  river  water  was  added. 
In  this  manner  the  prescribed  amount  of  alu 
minum  hydrate  was  added  in  the  form  of  larger 
initial  particles,  as  it  was  mixed  with  the  full 
quantity  of  water,  than  in  the  case  of  the 
second  portion. 

Samples  of  water  were  collected  for  analy 
sis  after  the  plan  stated  in  the  last  experiment. 

In  the  following  tables  are  summarized  the 
principal  analytical  results  obtained  from  each 
portion  of  water  treated  in  these  three  sets  of 
experiments. 

The  first  table  contains  the  percentages  of 
removal  from  the  water,  after  24  hours  subsi 
dence,  of  organic  matter,  as  indicated  by  al 
buminoid  ammonia  and  oxygen  consumed, 
respectively;  of  the  suspended  matter,  and  of 
the  bacteria. 

The  second  table  contains  the  results  of 
the  determination  of  the  respective  amounts 
of  suspended  matter  in  the  several  treated 
waters  of  experiments  Nos.  2  and  3,  atfer  sub 
sidence  for  different  periods. 

The  third  table  contains  the  number  of  bac 
teria  found  in  the  several  portions  of  treated 
water  in  experiments  Nos.  2  and  3,  after  dif 
ferent  periods  of  subsidence. 

SUMMARY  OF  ANALYTICAL  RESULTS  FROM 
THE  LAST  THREE  EXPERIMENTS,  SHOW 
ING  THE  PERCENTAGES  OF  REMOVAL  OF 
ORGANIC  MATTER,  SUSPENDED  MATTER, 
AND  BACTERIA,  AFTER  24  HOURS'  SUB 
SIDENCE. 
Percentage  Removal  of  Albuminoid  Ammonia. 


Number  of 

Por 

ion  of  Water  Trea 

ted. 

Kxperiment. 

Firs!. 

Second. 

Third. 

I 

2 

3 

f>4 
83 
43 

80 
93 
69 

55 
80 
58 

296 


WATER   PURIFICATION  AT  LOUISVILLE. 


Percentage    Removal   of  Oxygen   Consumed. 


Portion  of  Water  Treated. 

Number  of 

Experiment. 

First. 

Second. 

Third. 

I 

66 

87 

54 

2 

80 

92 

73 

3 

52 

67 

65 

Percentage  Removal  of  Suspended  Matter  of 

the  River  Water. 

i 

93 

IOO 

78 

2 

96 

100 

93 

3 

78 

96 

88 

Percentage  Removal  of  Bacteria. 

i 

37 

86 

37 

2 

74 

94 

57 

3 

39 

88 

73 

SUMMARY  OF  ANALYTICAL  RESULTS  FROM 
EXPERIMENTS  NOS.  3  AND  '3,  SHOWING  THE 
AMOUNTS  OF  SUSPENDED  MATTER  IN  THE 
WATER  AFTER  DIFFERENT  PERIODS  OF 
SUBSIDENCE. 

Experiment  No.  2. 


Period  of 
Subsidence. 
Hours. 

Parts  per  Million  of  Suspended  Solids. 

First  Portion. 

Second  Portion. 

Third  Portion. 

0 

5 
20 

I  397 
136 
60 

i  397 
5 
4 

I  397 
199 
99 

24 

52 

o 

99 

Experiment    No.    3. 


Period  of 

Parts  per  Million.  Suspended  Solids. 

Hours. 

First  Portion. 

Second  Portion. 

Third  Portion. 

0 

243 

243 

243 

6 

104 

33 

83 

20 

56 

13 

33 

24 

54 

10 

33 

SUMMARY  OF  ANALYTICAL  RESULTS  FROM 
EXPERIMENTS  NOS.  2  AND  !!,  SHOWING  THE 
NUMBERS  OF  BACTERIA  IN  THE  WATER 
AFTER  DIFFERENT  PERIODS  OF  SUBSI 
DENCE. 

Experiment   No.    2. 


Bacteria  per  Cubic  Centimeter  in  River  Water 

Period  of 

after  Treatment. 

Hours 

First  Portion. 

Second  Portion. 

Third  Portion. 

O 

I  7  600 

17600 

I  -  600 

5 

2O  700 

900 

T7400 

20 

5900 

600 

7700 

24 

4500 

I  2OO 

8  loo 

Experiment   No.   3. 


o 

25  600 

25  600 

25  600 

6 

18  200 

10  800 

1  8  900 

20 

16  700 

3  500 

7  ooo 

24 

15  600 

;  •_•<  i.  < 

7  ooo 

On  the  next  page  are  given  the  results  of 
chemical  analyses  of  the  original  river  water 
and  of  the  several  portions  of  treated  water 
in  each  experiment  after  subsidence  for 
24  hours.  As  already  stated,  samples  of  the 
treated  water  were  removed  from  the  bottles 
by  means-  of  a  siphon,  without  disturbance  of 
the  solid  matters  which  had  settled  to  the 
bottom. 

Attention  is  especially  called  to  the  fact  that 
the  electrolytically  produced  aluminum  hy 
drate,  as  well  as  that  prepared  in  the  labora 
tory,  did  not  decrease  the  alkalinity  of  the 
water.  This  means  that  no  carbonic  acid  gas 
was  set  free,  and  that  no  lime  passed  into  the 
form  of  sulphate,  because  the  formation  of 
this  compound  in  these  cases  was  independ 
ent  of  the  lime  in  the  water. 

The  samples  of  water  for  chemical-  analysis 
were  numbered  as  follows: 


Treated  Water  after  24  Hours'  Subsidence. 

Original 

Water. 

First  Portion. 

Second 

Third 

809 

810 

Sn 

812 

813 

814 

815 

816 

.         819 

820 

821 

THE  EFFECT  OF  THE  ACTION  OF  THE  ELEC 
TRO-MAGNETS  UPON  THE  CONSTITUENTS 
OF  THE  OHIO  RIVER  WATER  AND  UPON 
THE  RATE  AT  \VHICH  ALUMINUM  HY 
DRATE  is  FORMED  FROM  METALLIC 
ALUMINUM. 

So  far  as  could  be  learned  from  a  series  of 
experiments  directed  to  this  point  the  electro 
magnets  produced  no  appreciable  effect  in  the 
purification  of  the  Ohio  River  water,  either 
directly  or  indirectly,  by  facilitating  subsi 
dence  or  increasing  the  rate  of  formation  of 
aluminum  hydrate. 

RATE   AT   WHICH    ALUMINUM    HYDRATE    is 

FORMED  ELECTROLYTICALLY  FROM 

METALLIC  ALUMINUM. 

One  of  the  most  important  points  in  con 
nection  with  the  treatment  of  water  by  elec 
trical  devices  is  information  upon  the  cost 
of  the  production  of  aluminum  hydrate.  Tt 
was  definitely  known  that  the  rate  of  forma- 


INVESTIGATIONS  OF   THE  PRINCIPLES   OF    THE  HARRIS   DEVICES.      297 


RESULTS    OF    CHEMICAL    ANALYSES    OF    SAMPLES    DESCRIBED    AMOVE. 
(Parts  per  Million.) 


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loS    046 
108  .016 
074  .022 
loS  .020 
104  .026 
104  .010 
080  .010 
086  .010 

ooo 

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004 

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CO  2 
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5-3 
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.16 



tion  of  this  compound  would  be  proportional 
to  the  strength  (amperage)  of  the  current,  pro 
vided  no  irregularities  occurred.  But  ade 
quate  data  were  lacking,  both  with  regard  to 
the  rate  of  formation  and  to  the  likelihood 
of  irregularities  such  as  would  affect  the  cost 
and  efficiency  of  the  treatment. 

In  the  course  of  54  experiments,  which 
were  made  during  the  first  three  weeks  in 
August,  attention  was  directed  to  this  point 
so  far  as  was  practicable.  The  experiments 
were  made  in  glass  jars  of  one  gallon  capac 
ity  and  in  the  porcelain-lined  tanks  described 
in  the  last  chapter.  Early  in  the  work  it  was 
learned  that  the  quality  of  the  water  appar 
ently  exerted  little  or  no  influence  upon  the 
rate  of  formation  of  aluminum  hydrate,  or  the 
influence  of  other  factors  disguised  its  effect. 
In  a  majority  of  cases  river  water,  from  which 
the  suspended  matters  had  been  removed  by 
filtration,  was  employed.  The  amount  of 
aluminum  hydrate,  which  was  formed  under 
certain  recorded  conditions,  was  determined 
both  by  weighing  the  amount  of  hydrate 
formed  and  by  noting  the  decrease  in  the 
weight  of  the  metallic  aluminum  electrodes. 

Several  important  observations  were  made 
as  to  the  manner  in  which  the  aluminum  hy 
drate  was  formed.  When  both  electrodes 
were  of  metallic  aluminum  the  electric  cur 
rent  caused  the  hydrate  to  appear  at  both 
poles,  but  for  the  most  part  at  the  positive 
pole.  A  considerable  quantity  of  gas  was 
liberated  at  the  negative  pole.  Gas  was  also 
set  free  at  the  positive  pole,  but  less  uniformly 


and  only  about  .20  per  cent,  of  the  volume  of 
that  which  came  from  the  negative  pole. 
Analyses  of  the  gas  from  the  negative  pole 
showed  it  to  be  practically  all  hydrogen.  If 
there  were  any  oxygen  (in  excess  of  that  com 
ing  from  the  atmosphere),  ozone,  or  hydro 
gen  peroxide  present  in  the  water  or  gas,  the 
quantities  were  so  small  that  they  escaped  de 
tection.  Upon  shutting  off  the  electric  cur 
rent  and  allowing  the  electrodes  to  remain 
in  the  treated  water  it  was  repeatedly  noted 
that  aluminum  hydrate  continued  to  appear 
for  20  seconds  or  more  after  the  current 
ceased.  This  observation  in  connection  with 
other  information  indicated  that  the  electric 
current  does  not  form  the  hydrate  directly 
from  the  metallic  aluminum,  but  it  prepared 
the  water  by  partial  decomposition  so  that 
certain  constituents  of  the  water  were  able  to 
produce  the  aluminum  hydrate. 

When  an  electric  current  had  passed 
through  the  aluminum  electrodes  for  several 
hours  it  was  found  that  the  positive  poles  be 
came  coated  with  aluminum  oxide  (aluminum 
rust),  and  that  from  time  to  time  this  coating 
fell  off  in  the  form  of  scales  of  a  considerable 
size  and  number.  At  the  negative  poles 
there  appeared  a  fine  black  coating,  which  was 
found  to  be  composed  of  minute  particles 
of  aluminum  in  a  (spongy)  metallic  state. 
From  an  economical  and  practical  point  of 
view  these  observations  have  considerable 
significance,  as  will  be  shown  in  following 
sections. 

In  the  next  table  are  recorded  all  the  re- 


WATER   PURIFICATION   AT  LOUISVILLE. 


suits  of  determinations  of  the  rate  of  forma 
tion  of  aluminum  hydrate,  electrolytically. 
These  results  are  expressed  in  the  number  of 
grains  and  grams  of  aluminum  decomposed 
from  the  metal  electrodes  in  one  hour  for 
each  ampere  of  electric  current,  according  to 
the  conventional  method.  The  weights  of 
aluminum  hydrate  which  these  amounts  of 
metal  would  form  may  be  obtained  by  multi 
plying  the  respective  figures  by  2.85.  The 
results  were  obtained  from  small  electrodes 
(of  bright  metal  at  the  beginning  of  each  ex 
periment)  during  short  periods,  as  a  rule,  in 
order  that  the  maximum  results,  free  from  ab 


normal  irregularities,  might  be  obtained. 
The  irregularities  have  already  been  referred 
to  and  will  be  mentioned  again  beyond.  To 
make  a  comprehensive  study  of  them  on  a 
small  scale  was  impossible.  It  will  be  noted  that 
a  variety  of  combinations  of  electrodes  were 
tried.  The  experiments  whose  numbers  do 
not  appear  in  this  table  are  referred  to  the 
foregoing  portion  of  this  chapter.  The  tabu 
lations  are  self-explanatory,  except  that  it  is 
to  be  staled  that  chemical  symbols  are  used 
as  abbreviations  of  the  substances  used  as 
electrodes.  Thus,  Al  means  aluminum;  C, 
carbon;  and  Pt,  platinum. 


SUMMARY     OF      RESULTS     SHOWING     THE     RATE     OF     ELECTROLYTIC     DECOMPOSITION     OF 

METALLIC    ALUMINUM. 


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In  the  consideration  of  the  results  in  the 
foregoing  table  it  is  to  be  borne  in  mind  that 
the  amounts  of  metal  decomposed  include 
the  oxide  as  well  as  the  hydrate  of  aluminum; 
as  the  oxide  came  off  irregularly  in  films  or 
scales,  it  is  probable  that  the  h'.ghest  results 
are  associated  with  this  factor.  Concerning 
the  low  results,  the  utilization  of  electric  cur 
rent  in  the  formation  of  oxygen  at  the  posi 
tive  pole  appears  to  be  the  explanation  of 
them. 


Taking  the  average  of  all  these  experi 
ments,  it  is  found  that  rate  of  decomposition 
of  aluminum  was  equal  to  8.16  grains  or  0.53 
gram  per  ampere-hour.  The  entire  current 
used  in  this  set  of  experiments  was  50.42 
ampere-hours,  and  the  to'tal  amount  of  metal 
decomposed  was  395.3  grains  or  25.67  grams. 
Computing  the  rate  of  decomposition  on  this 
basis,  the  rate  of  7.84  grains  or  0.509  gram 
per  ampere-hour  is  obtained.  This  is  practi 
cally  an  exact  agreement  with  the  results  of 


INVESTIGATIONS   OF    THE  PRINCIPLES   OF    THE  HARRIS  DEVICES.      299 


Watt  ("  Electro-Deposition  of  Metals,"  page 
548),  who  states  that  the  rate  of  decomposi 
tion  of  aluminum  is  7.92  grains  or  0.514  gram 
per  ampere-hour. 

This  subject  is  taken  up  more  at  length  in 
Chapter  XV,  Section  No.  4,  where  an  ex 
planation  of  the  difference  between  the  above 
rate  of  decomposition  and  that  indicated  by 
the  electro-chemical  equivalent  of  aluminum 
is  offered. 

REGULARITY  DURING  CONTINUOUS  SERVICE 
OF  THE  RATE  AT  WHICH  ALUMINUM 
HYDRATE  is  FORMED  ELECTROLYTI- 

CALLY  FROM   METALLIC   ALUMINUM. 

When  the  metallic  aluminum  electrodes 
were  bright  and  clean  the  rate  of  formation 
of  aluminum  hydrate  per  ampere-hour,  with 
other  conditions  equal,  seemed  to  be  fairly 
uniform.  After  a  time,  however,  the  positive 
pole  became  coated  with  oxide  of  aluminum, 
and  the  rate  of  formation  of  the  hydrate  de 
creased.  In  time  this  coating  of  oxide  be 
came  so  thick  that  it  fell  off,  and  the  rate 
temporarily  increased. 

On  a  large  scale  of  operation  this  would 
doubtless  be  an  important  matter  for  consid 
eration.  From  the  available  evidence,  with 
runs  of  not  more  than  five  hours,  variations 
of  20  per  cent,  in  the  formation  of  aluminum 
hydrate  per  ampere-hour  were  noticed,  when 
the  conditions  other  than  the  coating  on  the 
electrodes  were  apparently  parallel. 

AMOUNT  OF  METALLIC  ALUMINUM  WHICH  is 
WASTED    IN   THE    ELECTROLYTIC    PRO 
DUCTION  OF  ALUMINUM  HYDRATE. 

Upon  passing  electricity  through  alu 
minum  electrodes  this  metal  passes  into  three 
different  forms: 

1.  Aluminum    hydrate    which    appears    at 
both  poles,  but  for  the  most  part  at  the  posi 
tive  pole.     It  is  this  form  which  serves  in  the 
purification  of  water  as  has  been  described 
and  discussed. 

2.  Some  of  the  metal  passes  into  the  solu 
tion  and   is  deposited   at  the  negative  pole. 
This  is  probably  deposited  in  a  spongy  metal 
lic  state  somewhat  similar  to  that  noted  under 
some  conditions  with  other  metals  in  electro 
plating.     The   amount   of   the   metal   which 


passes  into  this  state  is  very  small  as  far  as 
could  be  learned. 

3.  After  the  positive  pole  has  been  in  ser 
vice  for  some  time  it  becomes  coated  with  a 
layer  of  aluminum  oxide,  which,  as  stated 
above,  gradually  becomes  thicker  until  it 
scales  and  falls  off.  The  aluminum  oxide 
serves  no  purpose  in  water  purification  and  is 
a  waste  product  which  would  be  expensive  in 
a  large  plant. 

The  results  of  the  experiments  show  that 
the  amount  of  metallic  aluminum  which  was 
wasted  by  passage  into  the  oxide  state  ranged 
from  25  to  40  per  cent,  of  that  which  was 
converted  into  the  form  of  aluminum  hydrate. 
It  may  also  be  added  that  this  was  borne  out 
by  the  experiences  with  the  devices  operated 
in  July.  In  two  instances  during  the  last  week 
in  July  where  the  periods  of  observed  opera 
tion  were  5  and  20  hours,  the  percentages  of 
metallic  aluminum  which  were  wasted  were 
estimated  to  be  51  and  53.  respectively. 

A  COMPARISON  OF  THE  COST  OF  ALUMINUM 
HYDRATE  FORMED  BY  THE  APPLICATION 
OF  SULPHATE  OF  ALUMINA  TO  \VATER, 
AND  BY  THE  ACTION  OF  ELECTRICITY  ON 
METALLIC  ALUMINA,  RESPECTIVELY. 

It  has  already  been  stated  that  of  the  two 
methods  of  production  of  aluminum  hydrate 
the  electrolytic  one  furnished  a  product  which 
was  less  efficient  in  the  coagulation  and  sedi 
mentation  of  the  Ohio  River  water,  and  which 
was  associated  with  a  wastage  of  25  to  40  per 
cent,  of  the  metallic  aluminum  from  which  it 
was  prepared.  Aside  from  the  question  of 
cost  of  power  to  produce  aluminum  hydrate 
electrolytically,  which  is  referred  to  in  the 
next  section,  there  is  a  marked  difference  in 
the  cost  of  the  commercial  product  used  in  the 
two  methods  of  preparation  of  aluminum  hy 
drate. 

Current  quotations  (Aug.,  1896)  give  the 
cost  of  metallic  aluminum  and  sulphate  of  alu 
mina  as  56  and  1.5  cents  per  pound,  respec 
tively.  To  produce  100  pounds  of  aluminum 
hydrate  by  the  two  methods  it  would  require 
35  pounds  of  metallic  aluminum  and  420 
pounds  of  sulphate  of  alumina  of  average 
composition,  respectively.  The  cost  of  these 
two  commercial  products,  on  the  above  basis, 
would  be  $19.60  and  $6.30,  respectively.  The 


300 


WATER   PURIFICATION  AT  LOUISVILLE. 


facts  show  conclusively  that  electrolytically 
prepared  aluminum  hydrate  is  more  than 
three  times  as  expensive  as  that  prepared 
from  sulphate  of  alumina,  independent  of  the 
wastage  of  metallic  aluminum  and  the  cost 
for  electric  power. 

OBSERVATIONS  ON  THE  AMOUNT  OF  POWER 
WHICH  WOULD  BE  REQUIRED  TO  PRO 
DUCE  ALUMINUM  HYDRATE  ON  A  LARGE 
SCALE  BY  MEANS  OF  ELECTRICITY. 

In  the  purification  of  the  Ohio  River  water 
by  the  aid  of  aluminum  hydrate  prepared  by 
the  two  methods  under  consideration,  the  first 
point  of  practical  importance  which  suggests 
itself  is  this  one:  The  electric  method  would 
require  boilers,  engines,  and  a  generating 
plant  large  enough  to  supply  the  needful 
amount  of  aluminum  hydrate  when  the  water 
is  muddiest,  while  in  the  other  method  such 
a  condition  of  the  water  would  require  in  ad 
dition  to  the  normal  appliances  simply  a 
stronger  solution  of  sulphate  of  alumina  and 
a  more  rapid  addition  of  the  chemical  solu 
tion. 

To  estimate  the  amount  of  electric  power 
necessary  for  the  formation  of  aluminum  hy 
drate  from  metallic  aluminum  in  the  purifica 
tion  of  the  Ohio  River  water,  the  necessary 
quantity  (amperage)  and  electric-motive  force 
(potential)  of  the  current  must  be  known. 
The  formation  of  hydrate  is  proportional  to 
the  amount  (amperage)  of  current  and. data 
on  this  point  are  presented  in  the  foregoing 
tables. 

\Yith  regard  to  the  voltage  (corresponding 
to  pressure  in  hydraulics)  necessary  in  a  plant 
on  a  large  scale,  this  cannot  be  stated  from 
the  evidence  available  at  this  time.  It  would 
doubtless  be  much  less  than  210,  however, 
which  was  the  voltage  supplied  to  the  devices 
operated  by  the  Harris  Company. 

As  a  matter  of  convenience  and  record,  it 
may  be  stated  that  to  treat  one  million  gal 
lons  of  water  in  24  hours  with  electrolytically 
prepared  aluminum  hydrate  equivalent  to  one 
grain  per  gallon  of  sulphate  of  alumina,  the 
number  of  horse-power  of  electricity  actually- 
used,  according  to  these  tests,  would  be  about 
one-half  the  potential  of  the  current. 


CONCLUSIONS. 

From  these  investigations  made  in  August 
upon  the  purification  of  the  Ohio  River  water 
by  electricity  the  following  conclusions  may 
be  drawn: 

1.  The  direct  application  of  electricity  and 
electro-magnets,    as    used    in    these    devices, 
produced   no   substantial    purification   of   the 
Ohio  River  water. 

2.  The  electrolytic  formation  of  aluminum 
hydrate  in  the  Ohio  River  water  enabled  sub 
stantial  purification  to  be  effected,  provided 
sedimentation     and     filtration     were     subse 
quently  employed,  as  was  similarly  done  by 
the  other  systems  investigated  in  these  tests 
and  whic'h  used  aluminum  hydrate  obtained 
from  the  application  of  sulphate  of  alumina. 

3.  The  use  of  electrolytically  prepared  alu 
minum  'hydrate  has  the  advantage  of  the  ap 
plication  of  sulphate  of  alumina  in  the  follow 
ing  points,  as  was  indicated  to  be  the  case  by 
the  operation   of  the  devices   of   the   Harris 
Company  in  July,  as  stated  at  the  close  of 
Chapter  XL 

A.  No  lime  in  the  river  water  is  required 
for  the  successful  application  of  the  process. 

B.  There  is  no  opportunity  of  getting  dis 
solved  chemicals  into  the  filtered  water. 

C.  There  is  liberated  no  carbonic  acid  gas, 
which  in  time  might  injure  boilers  and   dis 
tributing   pipes. 

/.).  There  is  dissolved  in  the  filtered  water 
no  additional  sulphate  of  lime,  which  at  times 
might  give  annoyance  and  trouble  when  the 
water  is  used  in  boilers. 

4.  For  the  purification  of  the  Ohio   River 
water  on  a  large  scale  the  electric  method,  as 
compared  with  the  method  in  which  sulphate 
of  alumina  is  used,  is  not  a  commercial  suc 
cess  because  of  its  excessive  cost. 

During  1897  some  further  investigations 
under  different  conditions,  in  connection  with 
the  use  of  metallic  aluminum  electrolytically 
decomposed  for  the  coagulation  of  the  Ohio 
River  water,  were  made  by  the  Water  Com 
pany.  The  results  of  these  investigations  are 
recorded  in  Chapter  XV,  but  it  may  be  noted 
here  that  the  conclusions  given  in  this  chapter 
were  confirmed. 


THE  MARK   AND   B  ROW  NELL   ELECTROLYT1CAL   DEVICES. 


CHAPTER   Xlil. 

DESCRIPTION  OF  THE  MARK  AND  BROWNELL  ELECTROLYTICAL  DEVICES,*  AND  A  RECORD 
OF  THE  RESULTS  ACCOMPLISHED  THEREWITH. 


AFTER  devoting  the  early  part  of  Decem 
ber,  1896,  largely  to  investigations  on  the  in 
creased  corroding  and  incrusting  power  of 
water  which  had  been  treated  with  sulphate 
of  alumina,  attention  was  again  directed  to 
methods  of  preparing  coagulants  by  electro 
lytic  means,  whereby  the  use  of  commercial 
sulphates  might  be  avoided. 

Several  Louisville  gentlemen  called  the  at 
tention  of  the  Water  Company  at  this  time  to 
some  electrolytical  experiments  upon  water 
purification,  which  had  been  in  progress  for 
several  weeks.  At  their  request,  the  directors 
and  officers  of  the  Water  Company,  on  Dec. 
21,  1896,  inspected  the  operation  of  two  small 
experimental  devices  along  this  line,  which 
were  operated  by  Profs.  Palmer  and  Browne!! 
in  their  laboratory  at  the  Louisville  Manual 
Training  High  School.  Among  the  other 
gentlemen  interested  in  these  experiments 
was  Prof.  Mark,  who,  with  Prof.  Brownell, 
had  been  retained  in  consultation  upon  elec 
trical  matters  by  the  Harris  Company  in  July. 
1896;  and  in  this  way  they  were  introduced 
to  the  electrical  and  electrolytical  treatment 
of  the  Ohio  River  water. 

The  object  of  these  devices,  and  of  their 
operation,  was  to  indicate  the  relative  merits 
of  the  application  of  electricity  to  electrodes 
composed  of  metallic  iron  and  metallic  alu 
minum,  respectively,  in  the  preliminary  treat 
ment  of  the  Ohio  River  water,  in  order  to  se 
cure  coagulation  in  a  system  of  purification, 
of  which  filtration  through  sand  is  the  last 
step. 

A  general  idea  of  these  two  devices,  which 
were  intended  to  be  duplicates,  with  the  ex 
ception  of  the  metal  used  for  the  electrodes, 
may  be  obtained  from  the  following  outline: 


Tap  water  (which  was  equivalent  to  Ohio 
River  water  from  which  a  portion  of  the  sus 
pended  matter  had  been  removed  by  passage 
through  the  Crescent  Hill  Reservoir  and  some 
of  the  distributing  pipes)  was  led  through  a 
meter  to  two  glass  cylinders,  each  about  4 
inches  in  diameter,  and  i.^  to  J.o  feet  in 
height.  On  the  top  of  each  cylinder  there  was 
fastened  a  suitable  cover,  in  which  were  per 
forations  for  the  glass  inlet  and  outlet  pipes, 
respectively.  The  glass  cylinders  of  the  two 
devices  contained,  respectively,  metallic  iron 
and  metallic  aluminum  electrodes,  which  were 
fairly  similar  in  shape  and  size.  In  each  case 
the  electrodes  were  made  of  sheets  fastened 
together,  about  0.5  inch  apart,  with  suitable 
insulating  materials.  The  electric  current  was 
supplied  by  a  dynamo  generator.  The  water 
was  admitted  to  the  cylinders  at  the  top,  and 
was  drawn  off  at  the  bottom.  A  second  perfor 
ation  in  each  of  the  covers  contained  a  glass 
tube,  to  which  a  rubber  tube  was  attached. 
Each  rubber  tube  was  controlled  by  a  clamp, 
so  that  from  time  to  time  the  gas,  which  ac 
cumulated  at  the  top  of  the  cylinders,  could  be 
removed.  From  the  glass  cylinders  of  the  two 
devices,  the  water  passed  to  t'he  respective  fil 
ters.  Each  filter  was  made  by  putting  a  layer 
of  fine  sand  in  a  metal  cylinder,  about  6  inches 
in  diameter,  and  2  to  3  feet  high.  It  was  said 
that  each  filter  contained  about  i  foot  of  fine 
sand,  beneath  which  were  several  inches  of 
coarse  sand,  and  a  metal  strainer,  which  was 
placed  above  the  outlet  at  the  bottom  of  the 
cylinders.  All  the  water  from  the  electro 
lytic  cells  (glass  cylinders)  passed  on  to  the 
filters,  but  in  each  case  a  considerable  portion 
of  the  treated  water  overflowed,  owing  to  the 
relatively  small  size  of  the  filters. 


Including  the  "  Palmer  and  Brownell  Water  Purifier,"  as  explained  beyond. 


302 


WATER   PURIFICATION  AT  LOUISVILLE. 


The  experiments  were  begun  before  the  ar 
rival  of  the  party  from  the  Water  Company. 
The  writer  understood  that  the  electrodes 'had 
been  weighed,  and  that,  in  the  case  of  the  iron 
device,  65  cubic  feet  of  water  had  been 
treated  after  weighing,  but  before  our  arrival. 
It  was  said  that  the  operation  of  the  aluminum 
device,  which  was  in  service  when  we  arrived, 
began  about  1.30  P.M.  This  device  was  op 
erated  until  about  4.10  P.M.  Before  this  time 
chemical  and  bacterial  samples  for  analyses 
were  collected  of  the  tap  water  before  treat 
ment,  of  the  electrolytically  treated  water  as 
it  overflowed  from  the  top  of  the  filter,  and  of 
the  effluent  as  it  passed  from  the  outlet  at  the 
bottom  of  the  filter.  The  time  required  to 
collect  a  gallon  of  this  effluent  was  30  min 
utes.  It  was  said  that  the  quantity  of  water 
passed  through  this  electrolytic  cell  from 
1.30  P.M.  to  4.10  P.M.,  was  30  cubic  feet.  The 
electric  current  varied  a  little  while  we  were 
present,  but  the  amperage  and  voltage  aver 
aged  3.6  and  32,  respectively. 

From  4.20  P.M.  to  4.50  P.M.,  about  7  cubic 
feet  of  water  were  passed  through  the  iron 
device.  The  amperage  and  voltage  averaged 
5.4  and  27,  respectively.  Samples  of  water 
for  analysis,  corresponding  to  those  taken 
from  the  aluminum  device,  were  collected, 
with  the  exception  of  the  tap  water.  The 
flow  of  water  through  the  filter  of  this  device 


was  much  faster  than  it  was  in  the  case  of 
the  other  filter.  This  filter  was  said  to  be  less 
satisfactory  in  its  construction  than  the  other 
one,  but  it  was  apparently  much  less  clogged 
at  the  surface.  It  required  7  minutes  to  fill 
a  gallon  bottle  with  this  effluent. 

In  the  case  of  each  electrolytic  cell,  the  for 
mation  of  gas  was  only  slightly  in  excess  of 
the  amount  which  was  absorbed  by  the  flow 
ing  stream  of  water,  and  only  a  very  small 
quantity  accumulated  at  the  top  of  the  cell. 

The  samples  were  taken  to  the  laboratory 
of  the  Water  Company  and  analyzed.  The  re 
sults  of  the  bacterial  analyses  are  given  in  the 
following  table,  in  which  reference  by  serial 
numbers  is  made  to  the  results  of  the  chemi 
cal  analyses,  as  stated  in  the  second  table. 

RESULTS  OF  BACTERIAL  ANALYSES. 


Source  of  Samp 

le 

Number  of 
Chemical 
Sample.* 

Number  of 
Haclerial 

Sample. 

Bacteria 
per  Cubic 
Centimeter. 

826 

Electrolytically  ( 
num)  treated 
before  filtratio 
The    same,    but 

ilumi- 
watcr, 

after 

827 
828 

4969 

6  500 
216 

Electrolytically 
treated  water, 

(iron) 
before 

The    same,     but 

after 

830 

*See 

lie  following 

table. 

RESULTS   OF   CHEMICAL   ANALYSES. 

(Parts   per   Million.) 


jg 

Nitrogen 

Residue  on 

Fixed  Residue 

. 

(j 

s 

as 

.a 

Evaporation. 

after  Ignition. 

i  '§ 

£  u 

0 

1 

Ammonia. 

i 

« 

«i 

< 

u 

Date.        Corresponding 

5  ~ 

° 

1      'S 

rt  w 

^  i: 

u 

•o 

D 

•n 

OJ 

V 

i8q6.               Bacterial 

E 

So 

fe 

2 

1 

.1 

V 

y. 

y- 

'§ 

a 

1 

•3 

| 

1 

| 

1 

c 

i/) 

H 

O 

U 

o 

H     x       a 

fe 

5 

H 

Q 

f~ 

« 

C5 

< 

Q 

« 

8-6 

Dec    2    '           4968 

,,| 

"8 

827 

4   6 

O88 

J 

828 

R-0 

"       2                   4970 

I    (.  .  . 

2.5 

.104 

.OOO 

.104 

.080 

.014 

0.84.9   137 

o 

137 

103        o 

103 

70.3 

0 

O.  I 

830 

"      2                    4972 

2 

2.6 

.112 

.000 

.  112 

.076 

.016 

0.84.9 

145 

0 

145 

no 

O 

no 

69.3 

o 

0.9 

The  above  data  indicate  that  the  amounts 
of  electric  power  used  in  the  iron  cell  and  the 
aluminum  cell  were  at  the  rate  of  197  and 
75  E.H.P.  per  million  gallons  per  24  hours, 
respectively.  From  the  loss  in  weight  of  the 
iron  and  aluminum  electrodes,  it  was  stated 
that  the  consumption  of  these  two  metals  was 


at  the  rate  of  86  and  60.7  pounds  per  million 
gallons,  respectively. 

It  is  estimated  from  the  above  data,  that 
the  amount  of  electric  current  applied  to  the 
water  in  its  passage  through  the  aluminum 
and  iron  devices,  was  equal  to  0.042  and  0.070 
ampere-hour  per  gallon,  respectively. 


THE  MARK  AND   BROWNELL   ELECTRO  LY  TIC  A  L   DEVICES. 


3°3 


The  analytical  results  show  that  with  the 
aluminum  device,  the  water  was  well  purified, 
but  in  the  case  of  t'he  iron  device,  due  in  part, 
apparently,  to  the  construction  of  the  filter, 
the  effluent  contained  some  iron,  and  a  high 
number  of  bacteria.  The  greater  part,  if  not 
all,  of  this  iron  apparently  came  from  the  silt 
in  the  tap  water,  and  not  from  the  electrodes. 

Taking  the  results  of  these  experiments  in 
general  terms,  it  may  be  stated  that  they  were 
on  too  small  a  scale,  and  of  too  short  dura 
tion,  to  convey  any  practical  specific  informa 
tion  on  the  purification  of  the  Ohio  River 
water,  other  than  that  iron,  a  comparatively 
cheap  metal,  may  be  electrolytically  decom 
posed  in  a  manner  similar  to  aluminum  with 
the  formation  of  a  gelatinous  hydrate,  capable 
of  coagulating  the  mud,  silt,  and  clay  in 
water. 

PLANS  FOR  TESTING  THE  TREATMENT  OF 
THE  OHIO  RIVER  WATER  ELECTRO 
LYTICALLY  WITH  THE  USE  OF  IRON 

ELECTRODES. 

Arrangements  were  completed  on  Jan.  i, 
1897,  whereby  the  Water  Company  should 
te.st  the  practicability  of  an  experimental  sys 
tem  of  water  purification,  the  electrical  appli 
ances  of  which  were  to  be  designed  by,  and 
constructed  under  the  supervision  of,  Profs. 
Mark  and  Brownell.  This  experimental  sys 
tem  included  a  set  of  appliances  which  would 
enable  250,000  gallons  of  river  water  to  be 
treated  electrolytically  with  iron  electrodes, 
in  order  to  secure  coagulation,  preparatory 
to  filtration.  As  a  matter  of  convenience,  it 
was  arranged  with  the  O.  H.  Je\vell  Filter 
Company  to  make  use  of  their  test  filter, 
which  at  that  time  was  the  only  one  remain 
ing  at  the  pumping  station. 

Comparing  this  process  with  those  systems 
of  purification  which  were  tested  during  the 
preceding  year,  it  will  be  noted  that  with  the 
exception  of  the  magneto-electric  system,  the 
general  principles  of  the  methods  of  pro 
cedure  were  substantially  the  same,  in  that 
they  consisted  of  the  following: 

1.  Treatment  of  the  river  water  with  a  co 
agulating  chemical. 

2.  Partial  clarification  of,  and   removal  of 
suspended  matter  from,  the  treated  water  by 
subsidence  in  a  settling  chamber. 


3.  Rapid  filtration  of  the  coagulated  and 
partially  subsided  water  through  a  sand  layer. 

The  most  marked  feature  of  difference  in 
the  Mark  and  Brownell  devices,  from  the  or 
iginal  Jewell  System,  was  the  kind  and 
method  of  formation  of  the  coagulating 
chemical.  The  electricity  by  itself  does  prac 
tically  nothing  in  the  purification  of  the  river 
water.  Its  action  is  almost  wholly,  if  not  com 
pletely,  an  indirect  one,  in  preparing  a  coagu 
lating  chemical.  This  was  clearly  demon 
strated  in  the  devices  operated  in  July,  1896, 
by  the  Harris  Company,  and  investigated 
further  by  the  Water  Company  in  August, 
1896,  as  stated  in  the  two  preceding  chapters. 
The  preparation  of  hydrate  of  aluminum  by 
the  electrolytic  decomposition  of  metallic  alu 
minum,  was  found  to  possess  an  advantage 
as  a  coagulant  when  compared  with  hydrate 
of  alumina  prepared  from  the  decomposition 
of  sulphate  of  alumina  by  the  lime  which  is 
naturally  present  in  the  river  water,  in  that 
there  are  added  to  the  purified  water  no 
chemical  properties  to  corrode  iron  vessels, 
or  to  incrust  steam  boilers.  Hydrate  of  iron 
possesses  gelatinous  and  coagulating  proper 
ties  somewhat  similar  to  those  of  the  hydrate 
of  alumina.  [Metallic  iron  is  much  cheaper 
than  metallic  aluminum,  and  the  indications 
were  that  similar  advantages  in  the  coagula 
tion  of  the  Ohio  River  water  might  be  ob 
tained  electrolytically  in  this  manner,  at  a 
reduced  cost.  To  ascertain  the  efficiency  of 
this  process,  and  to  obtain  data  indicating  the 
cost  of  installation  and  of  operation  of  such  a 
system  for  the  purification  of  the  water  sup 
ply  of  this  city,  was  the  object  in  testing  the 
devices  of  Profs.  Mark  and  Brownell.  Ar 
rangements  were  made  whereby  Profs.  Mark 
and  Brownell  were  engaged  by  the  Water 
Company  to  design  and  superintend  the  con 
struction  of  the  necessary  electrical  devices. 
These  devices  in  connection  with  the  Jewell 
filter,  were  to  be  operated  and  tested  by  the 
Water  Company  under  the  direction  of  the 
Chief  Chemist  and  Bacteriologist,  but  Profs. 
Mark  and  Brownell  were  to  inspect  daily  the 
devices  designed  by  them,  and  make  such 
recommendations  as  seemed  advisable. 

The  time  from  Jan.  i  to  Feb.  12  was  oc 
cupied  in  constructing  electrodes,  electro 
lytic  cells,  and  a  dynamo  generator,  especially 


3°4 


WATER  PURIFICATION  AT  LOUISVILLE. 


adapted  to  this  class  of  work;  in  making  suit 
able  piping  and  electrical  connections;  and  in 
installing  an  engine  to  operate  the  generator. 
During  this  period,  considerable  attention 
was  given  to  the  practical  significance  of  sev 
eral  features  of  the  process,  so  far  as  the  avail 
able  appliances  permitted.  These  special  in 
vestigations  made  by  the  Water  Company 
during  this  unavoidable  delay  in  the  regular 
work,  are  recorded  in  Chapter  XVr. 

CONSTRUCTION  OF  THE  MARK  AND 

BROWNELL   DEVICES. 

The  devices  consisted  of  an  engine,  dynamo 
generator,  two  electrolytic  cells  and  two  sets 
of  electrodes,  in  addition  to  the  necessary  pip 
ing,  cables  and  wiring,  to  give  them  the 
required  water,  steam  and  electrical  connec 
tions.  The  electrolytic  cells  were  in  duplicate 
in  order  to  test  two  forms  of  electrodes.  One 
set  was  made  of  wrought-iron  plates,  designed 
by  Prof.  Brownell,  and  the  other  designed  by 
Prof.  .Mark,  was  made  of  cast-iron  pipes 
placed  within  each  other.  Each  cell  with  its 
set  of  electrodes  was  tested  separately,  in  con 
nection  with  the  Jewell  filter. 

It  may  be  added  here  that  these  electrolytic 
cells,  and  the  electrodes  which  were  made  ac 
cording  to  the  plans  of  Prof.  Brownell,  were 
found,  after  the  work  had  been  begun,  to  repre 
sent  "  The  Palmer  and  Brownell  Water  Puri 
fier — Patent  applied  for."  So  far  as  is  known, 
an  application  for  a  patent  for  the  devices  de 
signed  by  Prof.  Mark  was  not  made.  The 
tests  of  the  Water  Company  at  this  time, 
therefore,  included,  but  extended  beyond, 
that  of  the  "  Palmer  and  Brownell  Water 
Purifier/'  which  was  mentioned  in  the  intro 
duction  to  this  report.  For  this  reason  the 
more  comprehensive  expression  of  "  Mark 
and  Brownell  Devices  "  is  used  as  the  title  of 
this  chapter. 

The  principal  details  of  the  construction  of 
these  devices  were  as  follows: 

Engine. — The  engine  was  a  new,  horizontal, 
fly-wheel  machine  of  the  Atlas  make.  Its 
principal  dimensions  were  as  follows:  Di 
ameter  of  steam  cylinder,  11  inches;  length 
of  stroke,  14  inches;  diameter  of  fly  wheel,  4 
feet;  and  diameter  of  driving  wheel,  4  feet. 
The  speed  was  regulated  by  a  fly-wheel  cen 


trifugal  governor.  It  was  connected  to  the 
dynamo  generator  by  a  lo-inch  leather  belt. 

Dynamo-generator. — The  dynamo-genera 
tor,  driven  by  the  Atlas  engine,  was  made  by 
James  Clark,  Jr.,  &  Co.,  of  Louisville.  It  was 
a  direct,  four-pole,  compound  machine,  rated 
at  50  volts  and  400  amperes  at  a  speed  of  800 
revolutions  per  minute.  The  current  was 
regulated  with  the  aid  of  a  field  rheostat,  and 
could  be  controlled  at  practically  any  desired 
amperage  within  the  range  of  the  machine. 

Electrolytic  Cells. — The  two  duplicate  cells 
were  made  of  wrought-iron  plates,  0.25  inch 
thick.  The  main  body  of  the  cells  was  cylin 
drical  in  form,  2.5  feet,  in  diameter,  and  6.0 
feet  high.  At  the  top,  the  cells  were  capped 
by  a  dome-shaped  cover,  and  the  bottom  of 
each  was  in  the  shape  of  a  cone.  The  shell 
was  riveted  together  with  o.5-inch  rivets.  A 
flange  was  riveted  to  the  upper  edge  of  the 
plate,  to  form  a  connection  with  the  cover, 
which  was  bolted  to  it.  The  cover  was  a 
dome-shaped  iron  casting,  i.o  inch  thick,  30 
inches  in  diameter,  and  12  inches  high  on  the 
inside.  On  the  bottom  of  the  cover  was  a 
suitable  flange,  to  allow  the  cover  to  be  bolted 
to  the  shell.  In  the  center  of  the  cover  at  the 
top,  there  was  a  shoulder  suitably  tapped  for 
connection  with  the  inlet  water  pipe.  A  0.5- 
inch  pipe  with  a  valve  was  tapped  into  the 
cover,  to  enable  the  operator  to  blow  off  the 
gas  which  accumulated  at  that  point  when  the 
device  was  in  operation.  A  sight  gauge  was 
connected  to  the  cover,  also,  to  allow  the 
quantity  of  accumulated  gas  to  be  noted.  The 
conical  bottom  of  the  cell  was  of  wrought 
iron,  27  inches  in  diameter  and  12  inches 
deep  on  the  inside.  The  upper  portion  of 
the  cone  was  capped  with  a  short  cylin 
drical  shoulder,  by  which  the  conical  bot 
tom  was  riveted  to  the  main  shell.  At 
the  apex  of  the  cone  (the  bottom  of 
the  cell)  there  was  a  flange  for  connection 
with  the  3-inch  blow-off  pipe.  The  4-inch 
outlet  pipe  was  connected  with  the  shell  by 
means  of  a  flange  joint  at  a  point  (>  inches 
above  the  bottom  of  the  cylindrical  portion 
of  the  cell,  and  extended  into  the  cell  about 
8  inches.  The  inner  surface  of  the  cell  con 
taining  the  Brownell  electrodes  was  covered 
with  a  heavy  coat  of  asphaltum  paint.  The 
inner  surface  of  the  other  cell  acted  as  part 


THE  MARK  AND   BROW  NELL   ELECTROLYT1CAL   DEVJCES. 


3°S 


of  the  negative  electrode,  and  was  not  in 
sulated. 

Brov.'iicll  Electrodes. — In  one  of  the  electro 
lytic  cells  the  manifold  of  wrought-iron  plates, 
designed  by  Prof.  Brownell,  was  placed.  The 
other  cell  contained  the  Mark  electrodes, 
which  are  described  in  the  following  sec 
tion: 

The  Brownell  electrodes  were  made  of  28 
wrought-iron  plates,  each  0.25  inch  thick,  and 
50.375  inches  long.  The  manifold  was  ar 
ranged  in  two  sections  of  9  plates  each,  and 
one  section  of  10  plates.  Of  these  sections, 
the  middle  one  was  made  of  10  plates  of  prac 
tically  the  same  width,  24  inches.  But  the 
width  of  the  plates  in  each  of  the  two  outer 
sections  ranged  from  22  to  10  inches,  in  order 
to  keep  the  distance  between  the  inner  per 
iphery  of  the  cell  and  the  edge  of  the  plates 
approximately  uniform.  The  plates  of  each 
section  were  fastened  together  by  six  0.75- 
inch  bolts,  which  were  covered  with  hard  rub 
ber  tubes  to  secure  insulation.  On  these  hard 
rubber  tubes  were  placed  hard  rubber  wash 
ers,  0.5  inch  thick,  to  serve  as  insulating  dis 
tance  pieces  in  keeping  the  plates  separated 
from  each  other.  All  three  sections  of  the 
manifold  were  supported  on  a  frame  of  oak, 
made  of  four  2-  by  4-inch  pieces.  This  frame 
itself  rested  on  an  angle  iron  at  the  bottom 
of  the  cell,  and  had  suitable  appliances  at 
tached  to  it  to  aid  in  lifting  the  electrodes 
out  of  the  cell.  The  space  between  the  sec 
tions  of  the  manifold  was  2  inches. 

The  total  area  of  one  side  of  these  plates 
was  27,400  square  inches,  and  the  cross- 
section  of  the  electrolyte  (the  water 
between  the  plates)  was  22,400  square 
inches. 

On  Feb.  26,  1897,^11  annular  wooden  frame 
was  put  into  the  cell  just  above  the  top  of  the 
electrodes,  to  fill  the  space  between  the  elec 
trodes  and  the  wall  of  the  cell,  and  the  sup 
porting  frame  at  the  bottom  was  also  filled 
in  to  close  the  corresponding  space  there. 

Mark  Electrodes. — These  consisted  of  ten 
pieces  of  cast-iron  water-pipes,  and  of  the  wall 
of  the  electrolytic  cell  in  which  they  were 
placed.  They  were  42  inches  long,  and  i,  3,  6, 
9, 12, 15, 18,  21,  24,  and  27  inches  in  diameter, 
respectively.  At  the  bottom  of  the  cell  was 
a  frame  of  2-  by  4-inch  oak  pieces,  resting  on 


an  angle  iron,  and  the  electrodes  were  placed 
on  this  frame.  The  electrodes  were  not  fas 
tened  together,  but  were  separated  from  each 
other  by  insulating  distance  pieces  of  vulcan 
ized  fiber.  The  distance  between  the  several 
pieces  of  pipe  ranged  from  0.5  to  1.5  inches, 
and  averaged  about  0.93  inch. 

With  regard  to  the  thickness  of  the  elec 
trodes,  there  was  also  considerable  variation, 
but  the  average  thickness  was  about  0.5  inch. 

The  total  superficial  area  of  one  side  of 
these  pipes  was  20,200  square  inches,  and  the 
cross-section  of  the  electrolyte  was  17,900 
square  inches. 

Electrical  Connections. — From  the  genera 
tor,  the  current  was  led  to  a  switch-board, 
where  an  automatic  circuit  breaker  and  a 
suitable  ammeter  and  voltmeter  for  measur 
ing  the  current  and  potential  were  provided. 
The  potential  of  the  dynamo  was  regulated  by 
means  of  a  rheostat  on  the  shunt  of  the  mag 
net  circuit.  Cables  conveyed  the  current  to 
the  two  cells.  At  no  time  were  both  cells 
used  at  the  same  time,  so  the  one  set  of  main 
connections  served  for  the  two.  In  the  case 
of  each  cell  there  were  two  openings  near  the 
top.  There  were  placed  in  these  openings 
wooden  plugs,  through  which  iron  bars  with 
binding  posts  at  each  end  were  driven.  These 
bars  formed  part  of  the  electrical  circuit,  and 
the  wooden  plugs  were  relied  upon  for  in 
sulating  them  from  the  cell.  To  the  outer 
binding  posts  the  cables  connecting  with  the 
switch-board  were  attached,  and  to  the  inner 
binding  posts  were  fastened  the  cables  con 
necting  the  anodes  (positive  plates)  and 
cathodes  (negative  plates),  respectively. 

In  the  case  of  the  Brownell  electrodes,  the 
plates  were  connected  with  the  cable  by 
means  of  a  brass  lug  bolted  to  each  plate. 
The  corners  of  the  alternate  plates  on  each 
upper  side  were  cut  off,  to  give  ample  space, 
and  the  two  cables  were  passed  through  and 
soldered  into  the  holes  in  the  brass  lugs,  which 
were  bolted  on  to  the  uncut  corners  of  the 
plates.  In  this  way  every  other  plate  was 
made  positive  or  negative,  as  the  case  might 
be.  To  arrest  electrolytic  action  on  the  brass 
lugs  and  the  copper  cable,  they  were  coated 
with  insulating  paint. 

In  the  case  of  the  Mark  electrodes,  the  two 
cables  attached  to  the  inner  binding  posts  of 


306 


WATER   PURIFICATION  AT  LOUISVILLE. 


the  cell,  were  connected  with  alternate  pipes 
by  means  of  brass  lugs,  in  a  manner  quite 
similar  to  that  used  on  the  Brownell  elec 
trodes.  The  outer  wall  of  the  cell  was  one  of 
the  plates  forming  the  cathode  (negative 
pole). 

Piping. — Each  of  these  electrolytic  cells 
was  provided  with  4-inch  piping  and  fittings, 
so  that  the  river  water  entered  the  cells  at  the 
top,  and  left  them  at  the  side  near  the  bot 
tom,  and  passed  to  the  settling  basin  below 
the  Jewell  filter,  which  was  operated  as  usual, 
except  that  the  application  of  sulphate  of  alu 
mina  was  omitted.  At  the  conical  bottom  of 
these  cells,  there  was  a  3-inch  blow-off  pipe 
leading  to  the  sewer. 

All  of  these  pipes  were  provided  with  valves 
and  meters  wherever  necessary,  and  the  only 
remaining  points  worthy  of  mention  are  the 
devices  at  the  inlets  of  the  cells,  to  facilitate 
the  distribution  of  the  river  water  between  the 
electrodes.  In  the  cell  containing  the  Brown- 
ell  electrodes,  there  was  attached  to  the  inlet 
pipe  a  cast-iron  dome,  24  inches  in  diameter, 
and  8  inches  high.  It  was  screwed  on  to  a 
nipple  which  was  connected  to  a  flange  on 
the  cover  of  the  cell.  The  plate  which  formed 
the  base  of  the  dome  was  slotted  to  cor 
respond  with  the  water  spaces  between  the 
electrodes,  and  in  setting  the  electrodes  in 
place,  care  was  taken  to  have  the  water  spaces 
and  the  slots  in  the  dome  come  opposite  each 
other.  The  base  of  the  dome  was  3.5  inches 
above  the  top  of  the  electrodes.  A  similar 
dome  was  attached  to  the  inlet  pipe  in  the 
cover  to  the  other  cell,  containing  the  Mark 
electrodes.  In  this  case,  however,  the  base  of 
the  dome,  which  was  12  inches  above  the  top 
of  the  electrodes,  was  perforated  with  forty 
o. 5-inch  'holes,  arranged  uniformly  over  the 
plate. 

Operation  of  the  Mark  and  Brownell  Devices — 
Brownell  Electrodes. 

These  devices  and  appurtenances  were 
assembled  together  ready  for  operation  on 
Feb.  12,  1897.  On  the  afternoon  of  Feb.  13, 
and  the  whole  day  of  Feb.  15,  the  devices 
were  in  preliminary  operation,  and  the  Jewell 
filter  was  washed  five  times  with  filtered  water 
to  put  it  in  normal  condition,  following  a  long- 


period  of  rest.  Official  operation  began  on 
Feb.  1 6.  The  rate  of  electrolytic  treatment, 
and  of  filtration,  was  to  be  250,000  gallons  per 
24  hours,  or  23.2  cubic  feet  per  minute.  A 
brief  general  account  of  the  operations  will 
now  be  given,  followed  by  a  summary  of  the 
principal  data,  including  the  results  of  an 
alyses  of  the  river  water  before  and  after 
treatment. 

The  river  water  was  fairly  muddy  at  this 
time;  while  the  filtered  water  was  not  of  sat 
isfactory  appearance  or  quality,  and  showed 
marked  signs  of  insufficient  coagulation  to 
secure  satisfactory  results  under  these  condi 
tions.  The  average  voltage  and  amperage  on 
Feb.  1 6,  were  37  and  450,  respectively;  and 
on  Feb.  17,  these  figures  were  32  and  395. 
On  the  evening  of  Feb.  17,  it  was  necessary 
to  stop  operations,  in  order  to  make  some  re 
pairs  and  modifications  on  the  dynamo  gen 
erator.  The  dynamo  generator  was  not  ready 
for  operation  again  until  Feb.  22,  and  the 
tests  were  suspended  during  the  intervening 
time. 

Mud,  iron  hydrate  formed  from  the  electro 
lytic  decomposition  of  the  electrodes,  and  a 
limited  amount  of  other  suspende'd  matter, 
such  as  silt,  clay,  and  bacteria,  accumulated 
in  the  conical  bottom  of  the  cell  beneath  the 
outlet  pipe  during  operation,  and,  at  Prof. 
Brownell's  request,  about  2  cubic  feet  of  this 
liquid  and  solid  material  were  blown  off  into 
the  sewer  once  an  hour.  The  accumulation 
of  gas  at  the  top  of  the  cell  was  also  blown 
off  hourly,  to  prevent  the  electrodes  from  be 
coming  uncovered  and  consequently  out  of 
active  service. 

Operations  were  resumed  on  Feb.  22,  at 
12.38  P.M.,  following  the  repairs  of  the  dy 
namo.  The  filter  was  washed,  and  the  water 
and  mud  removed  from  the  settling  chamber 
of  the  Jewell  System.  The  rate  of  treatment 
and  of  filtration  was  23.2  cubic  feet  per  min 
ute,  as  provided  for  in  the  plans  and  designs. 
But  the  filtered  water  was  very  turbid  and  un 
satisfactory  in  appearance,  and  at  1.55  P.M., 
operations  were  stopped,  and  the  filter  washed 
again.  The  devices  were  then  started  at  the 
rate  of  15  cubic  feet  per  minute.  As  the  fil 
tered  water  did  not  improve  materially  in  ap 
pearance,  the  rate  was  reduced  to  about  12 
cubic  feet  at  4.00  P.M.,  and  at  5.00  P.M.  it  was 


THE  MARK  AND   BROW  NELL   ELECTROLYTICAL   DEVICES. 


3°7 


further  reduced  to  about  10  cubic  feet  per 
minute.  During  the  afternoon,  the  current 
was  approximately  constant,  and  the  voltage 
and  amperage  averaged  27  and  402,  respect 
ively.  At  no  time  was  the  filtered  water  free 
from  a  distinct  muddy  appearance,  although 
the  removal  of  coarse  suspended  particles 
caused  it  to  look  much  better  than  the  un 
treated  river  water. 

On  the  morning  of  Feb.  23,  the  devices 
were  operated  for  a  short  period  at  the  rate 
of  13  cubic  feet  per  minute,  but  the  electro 
lytic  treatment,  under  the  existing  conditions, 
was  insufficient  to  give  satisfactory  results. 
The  river  water,  however,  was  exceedingly 
muddy  at  this  time,  which  was  the  early  por 
tion  of  a  period  of  a  very  heavy  flood  in  the 
Ohio  River.  During  the  balance  of  this  day, 
and  during  the  following  day,  Feb.  24,  the 
devices  were  operated  at  the  rate  of  4.9  and 
9.8  cubic  feet  per  minute,  respectively.  On 
both  days  the  quantity  of  electric  current  was 
as  great  as  the  appliances  would  allow  (400 
amperes),  but  the  filtered  water  was  decidedly 
muddy.  i 

As  it  was  clearly  evident  that  these  devices 
were  unable  to  purify  the  Ohio  River  water 
when  it  was  in  the  existing  condition,  and 
further  tests  without  modifications  would  be 
a  waste  of  time  and  money,  the  writer  re 
ported  the  condition  of  affairs  to  President 
Long,  and  requested  instructions  in  the  prem 
ises,  as  follows: 

(Copy.) 

FEB.  25,  1897. 

Mr.  Chas.  R.  Long,  President  Louisville  Water 
Company,  Louisville,  Kentucky. 

DEAR  SIR:  Since  Monday  noon  of  this 
week,  we  have  operated  daily  the  electrical 
devices  designed  by  Profs.  Mark  and  Brown- 
ell,  with  the  view  to  purifying  the  present, 
very  muddy,  water  of  the  Ohio  River,  at  rates 
ranging  from  23.2  (contract)  to  5  cubic  feet 
per  minute.  At  no  time  have  we  obtained  an 
effluent  after  nitration  which  could  be  proper 
ly  called  purified,  or  which  could  be  compared 
with  our  earlier  results  during  this  series  of 
tests. 

So 'far  as  my  knowledge  goes,  whatever 
suggestions  that  may  have  been  made  by 
Profs.  Mark  and  Brownell,  have  been  fol 


lowed  out  in  the  operation  (A  these  devices, 
but  thus  far  I  have  received  no  formal  notice 
as  to  their  wishes  in  this  matter. 

In  view  of  the  fact  that  the  results  obtained 
from  these  devices  last  week  were  not  satis 
factory  with  regard  to  the  quality  of  the  fil 
tered  water,  and  that  the  results  of  this  week 
appear  to  be  of  no  practical  value  to  this  Com 
pany,  either  with  regard  to  capacity  to  handle 
this  water,  or  with  regard  to  its  satisfactory 
purification,  I  have  stopped  the  operation  of 
these  devices.  I  hereby  notify  you  officially 
of  the  present  conditions,  and  respectfully  re 
quest  instructions  in  the  premises. 

Very  respectfully, 
[Signed]        GEORGE  W.  FULLER, 

Chief  Chemist  and  Bacteriologist. 

On  Feb.  25,  the  makers  of  the  dynamo 
made  some  changes  in  the  machine,  as  recom 
mended  by  Prof.  Brownell.  Unofficial  tests 
showed  that  on  this,  and  several  following 
days,  there  was  a  marked  reduction  in  the 
maximum  amount  of  current  which  the  dy 
namo  could  put  through  the  electrolytic  cell. 
On  preceding  days,  500  amperes  could  be  ob 
tained  at  a  potential  of  about  40  volts.  It 
was  now  found  that  conditions  had  changed 
so,  that  with  55  volts,  the  maximum  potential 
of  the  machine,  only  about  375  amperes  of 
current  could  be  obtained.  The  devices  were 
carefully  examined  by  Profs.  Mark  and 
Brownell.  This  marked  reduction  of  45  per 
cent,  in  the  maximum  amount  of  current 
which  could  be  passed  through  the  electro 
lytic  cell,  when  the  dynamo  was  operated  at 
its  maximum  potential,  means  practically  a 
similar  increase  in  the  cost  of  electrolytic 
treatment  under  the  conditions  stated,  and  is 
a  factor  which  is  given  consideration  beyond 
in  the  discussion  of  these  results. 

At  the  request  of  Prof.  Brownell,  there  was 
placed  on  Feb.  26  an  annular  wooden  frame 
both  at  the  top  and  the  bottom  of  the  elec 
trolytic  cell,  in  order  to  reduce  the  space 
through  which  the  river  water  could  pass 
without  treatment. 

Profs.  Mark  and  Brownell  examined  the 
devices  on  Feb.  27,  and  requested  that  an  un 
official  run  be  made  with  the  maximum  elec 
tric  current,  and  a  rate  of  flow  of  water  of 
IO  cubic  feet  per  minute.  Their  request  was 


3o8 


WATER   PURIFICATION  AT  LOUISVILLE. 


complied  with.  But  in  spite  of  the  fact  that 
the  river  water  contained  only  about  one-fifth 
as  much  mud  as  was  the  case  earlier  in  the 
week,  it  was  not  possible,  even  at  this  low 
rate  of  treatment,  to  obtain  a  filtered  water 
which  was  not  muddy  in . appearance.  The 
Brownell  electrodes  were  not  used  again,  ex 
cept  in  some  special  comparative  experiments, 
as  requested  by  President  Long.  The  results 
of  analyses  of  the  water  before  and  after  treat 
ment,  with  summaries  of  the  principal  data 
and  discussions  thereon,  are  presented  be 
yond. 

The  devices  were  not  operated  again  until 
March  5.  when  the  second  electrolytic  cell, 
containing  the  Mark  electrodes,  was  used. 
The  rate  of  treatment, and  of  filtration,  was  10 
cubic  feet  per  minute  on  March  5,  and  on 
March  6  the  rate  was  5  cubic  feet.  On  both 
days  the  dynamo  was  run  at  the  maximum 
output  which  could  be  safely  handled.  The 
filtered  water,  however,  was  unsatisfactory  in 
appearance,  and  the  greater  water  space  be 
tween  these  electrodes  made  it  impossible, 
with  the  available  appliances,  to  secure  as 
much  coagulation  of  the  river  water  as  in  the 
case  of  the  Brownell  cell,  on  account  of  the 
decrease  in  current,  due  to  the  increased  re 
sistance  which  the  current  met  in  its  passage 
through  the  Mark  cell. 

As  i'rofs.  Mark  and  Brownell  formally  an 
nounced  at  this  time  that  they  had  no  further 
modifications  or  suggestions  to  make,  these 
devices  in  their  present  form  were  not  regu 
larly  operated  again. 

Sl'MMARY   AND    DlSCl'SSlON    OF  THE    RESULTS 

ACCOMPLISHED  BY  THE  MARK  AND 
BROWNELL  DEVICES. 

There  were  nine  official  runs  made  with  the 
devices  during  the  period  from  Feb.  16  to 
March  6.  Seven  of  these  runs  were  with  the 
Brownell  electrodes,  and  the  last  two  were 
with  the  Mark  electrodes.  In  the  case  of  the 
latter,  very  little  information  was  obtained, 
so  the  discussion  will  be  confined  to  the  re 
sults  obtained  from  operations  with  the 
Brownell  electrodes.  To  obtain  more  light 
upon  the  work  accomplished  by  these  devices, 
President  Long  requested,  first,  that  a  com 


parison  be  made  of  the  results  accomplished 
by  the  electrolytical  devices  with  the  Brownell 
electrodes  in  connection  with  the  Jewell  filter 
and  those  obtained  with  the  same  river 
water  by  this  filter  without  any  treat 
ment  whatever;  and,  second,  that  a  set 
of  aluminum  electrodes  be  made  to  duplb 
cate  the  iron  electrodes  designed  by  Prof. 
Brownell,  and  then  compare  the  results 
obtained  with  the  respective  electrodes,  in 
connection  with  the  Jewell  filter,  in  purifying 
the  same  river  water.  Owing  to  unavoidable 
delays  in  securing  aluminum  sheets,  these 
comparative  tests  were  not  completed  until 
April  4.  The  results  obtained  from  them  are 
recorded  just  beyond  this  discussion,  and  are 
followed  by  the  detailed  results  of  analyses  of 
samples  connected  with  the  tests  of  these  de 
vices. 

The  following  set  of  tables  contain  a  sum 
mary  of  the  principal  data  obtained  with 
reference  to  the  rate  of  treatment  and  filtra 
tion,  the  amount  of  electrolytic  treatment  em 
ployed,  the  amount  of  electric  power  used, 
and  the  degree  of  purification  after  the  treated 
river  water  had  passed  through  the  Jewell  fil 
ter,  and  also  the  results  of  bacterial  and  chem 
ical  analyses  of  the  individual  samples  of  the 
water  before  and  after  treatment. 

BACTERIA  PER  CUBIC  CENTIMETER  IN  THE 
OHIO  RIVER  WATER  TREATED  BY  THE 
MARK  AND  BROWNELL  DEVICES  AND  THE 
JEWELL  FILTER. 


Number  of 
Sample. 

Date. 

1897. 

Hour. 

Bacleria 
per  Cubic 

4973 

Feb.  16 

9.30  A.M. 

22  60O 

4975 

if> 

I.3O  P.M. 

25  TOO 

4979 

16 

4-30       " 

34000 

497ga 

17 

9.30  A.M. 

22  IOO 

4982 

17 

12.30  P.M. 

24  900 

4985 

17 

5-OO       " 

24  200    ' 

4986 

22 

9.30  A.M. 

20  500 

4989 

22 

2.35  r.M. 

60  400 

4992 

22 

5.OO       " 

59500 

4993 

23 

9.30  A.M. 

63400 

4996 

23 

12.30  P.M. 

59700 

4999 

23 

5.OO       " 

56  500 

5000 

24 

9.30  A.M. 

41  ooo 

5003 

24 

12.30  P.M. 

1  6  700 

5006 

24 

4-3°       " 

36500 

5039 

Mir.     5 

9.30  A.M. 

37900 

5041 

5 

4.30  P.M. 

28  700 

.    5056:1 

6 

11.30  A.M. 

31  500 

5058 

6 

2.OO  P.M. 

4J  ooo 

5061 

6 

5.00       " 

47  ooo 

THE  MARK  AND   BROWN  ELL   ELECTROLYTICAL    DEVICES. 


3°9 


SUMMARY   OF    RESULTS   ACCOMPLISHED    BY   THE    MARK    AND    BROWNELL    DEVICES. 


- 

et 

Began. 

Electric  Current. 

Quantities  of  Water. 
Cubic  Feet. 

Average  Rates  of 
Filtration. 

\ 

Date. 

'897- 

Hour. 

II.  I-    pc. 
Million       Ampere  Hours 
Gallons  per       per  Gallon. 

Filtered. 

Wash. 

!      Million 
Cubic  Feet   Gallons  per 
per  Minute.  ,    Acre  per 

X 

1  24  Hours. 

Brownell   Electrodes. 


I 

Feb.  16 

11.44  A.M. 

93 

0.044 

5383 

820 

22.6 

92 

3h 

,6m. 

2 

"     16 

4.05  P.M. 

73 

O.O4I 

6344 

595 

22.5 

91 

4h 

42m. 

3 

"     17 

1.22      " 

6 

5 

O.O40 

6273 

9-13 

23.0 

93 

4h 

33m. 

4 

"       22 

2.22      " 

9 

7 

0.064 

2574 

542 

14.0 

57 

31' 

O2m. 

5 

"       23 

9.52  A.M. 

121 

O.070 

626 

381 

13.0 

52 

oh 

48m. 

6 

"       23 

11.05      " 

28 

3 

0.181 

I  902 

455 

4-9 

20 

6h 

2511). 

7 

"       24 

9-52      " 

175 

0.091 

4  735 

674                9.8 

40 

Sh 

05m. 

Mark   Electrodes. 

\f          h    - 

4.2O  P.M. 

IQ 

A 

o  ooo 

711 

IO.  I 

41 

ih 

T  "km 

2 

"      6 

1.27      " 

iy~t 

384 

\j  .  vjv/y 

0.197 

I  08  1 

5-i 

2O 

3h 

33m. 

Estimated  Aver 

Nitrogen  a 

i  Albuminoid  Ammonia.                 Oxygen  Consumed. 

Average 

Bacteria 

sl 

age  Suspended       DeRree  of 

Pa 

r:s  per  Million.                                   Parts  per  Million. 

per  Cubic  Centimeter 

;  Average 

12 

3  0 

7. 

Solids  in  Ri.er        Clearness 
Water.     Harts      of  Effluent, 
per  Million. 

River 
Water. 

*""«"«•        Reeved'.       wile?.       Affluent.  ,££?£ 

River 
Water. 

Effluent. 

Bacterial 
Efficiency 

Brownell    Electrodes. 


I 

254 

3 

.326 

.  116 

64 

6.4                2.0 

69 

23  800 

5400 

77-3 

3  580 

86  7 

3 

308 

3 

.380 

.114 

7° 

6.8 

2.0 

71 

22  300 

3  78o 

83.0 

1                   474 

4 

-542 

.182 

66 

9-1            3-9 

57 

60000          8  ooo 

86.7 

4372 

4 

3-084 

.110 

96 

50.3            2.3 

95 

63  400 

4400 

93.1 

6 

4372 

4 

3.084            .110 

96 

50-3     .       =-4 

95 

58  100 

4  200 

92.8 

1 

3604 

4 

2.360     :        .084 

96 

48.9            2.5     :       95 

31  4CO 

4  260 

86.5 

Mark   Electrodes. 

i                  205 

5 

.762 

.260 

66 

12.0 

4-2 

65 

28  700 

7300 

74-5 

2                53"                     5 

4.900 

.  i-r 

96             65  i) 

3-0 

'): 

39  Soo        22  100 

44-6 

BACTERIA    PER    CUBIC    CENTIMETER    IN    THE   OHIO    RIVER    WATER    AFTER    TREATMENT    BY 
THE   MARK    AND    BROWNELL    DEVICES    AND    THE   JEWELL    FILTER. 


Rate  of 

41 

5! 

Collected. 

Filtration. 

£ 

'! 

'| 

n 

Number 

s. 

JSL 

r> 

Period  of 
ServiceSince 
Last 

2-jL 

u 

8 
2; 

Run. 

S.J 

6   0   3 

X 

Washing. 
Hours  and 

|lu 

*i 

Remarks. 

Date. 

Hour. 

u  1 

c  i.I 

"a 

Minutes. 

u   V-  .£3 

V   = 

•g 

1897. 

•§s 

3S.» 

£ 

f  a  3 
-J(J 

5u 

X 

u 

s 

J 

£ 

n 

Brownell    Electrodes. 

4974 

Feb.  16 

12.30  P.M.                     I 

23-5          95          4-7 

oh.  46m. 

I  241'     7  200 

4976             '      1  6 

1.30      "                        I 

23-5 

95          5-2 

Ih.  44m.        2  541      5  200 

4977             '      lf> 

2.30      "                        I 

23.5 

95 

2h.  44111. 

3  881     3  800 

49781             '     16 

4.30      "                       2 

23-5 

95 

3-5 

oh.  2501. 

588     4  400 

4980             '      17 

IO  2O  A.M.                    2 

23-5 

95 

8.2 

2h.  25m. 

3  244     3  090 

4981 

'     17 

1  2  .  30       "                         2 

23-5 

95 

8-4 

4h.  35111. 

6  068     3  250 

4983 

'      I/ 

2.30  P.M.                3 

23-5 

95 

4-4 

ih.  o8m. 

i  584     4  120 

4984 

"      17 

5.00     "                   3 

23.0 

93 

7-2 

3h.  3601. 

4964     3160 

4987 

"       22 

i-3»     "                   3 

23.0 

93 

7-7 

4h.  oSm. 

5738     4050 

"      22 

2-35     ' 

4 

20.0 

Si 

2.8 

oh.  13111. 

285     >  Km 

499° 

"      22 

3.30    " 

4 

16.0 

65 

2.7 

ih.  oSm. 

I    175     10  2(KI 

499  i 

"      22 

5.00     " 

4 

12.0 

48 

2.0 

2h.  35m. 

3  385     5  830 

4994 

"      23 

10-30  A.M. 

5 

IO.O 

41 

oh.  38111. 

380     4400 

4995 

"      23 

12.30  P.M. 

6 

5-o 

20 

0.4 

ih.  25m. 

424     4  700 

4997 

"      23 

2.30      " 

6 

5.0 

20 

0.4 

3h.  2501. 

980     4  030 

4998 

"      23 

5.00     " 

6 

5-0 

2O 

0-5 

5h.  55m. 

i  295     3  890 

5001 

"      24 

IO.3O  A.M. 

7 

IO.O 

41 

0-7 

ih.  O5m. 

645     3  050 

5002 

"      24 

I2.3O  P.M. 

7 

9-5 

40 

1-3 

3h.  05111. 

I  815     6000 

5004 

"      24 

2-30      " 

7 

IO.O 

41 

i.  g 

5h.  osm. 

3  005     4  400 

5005 

11      24                         4.30      " 

7 

IO.O 

41           2.8      7h.  05m. 

41551    3500 

Mark   Electrodes. 

5056 

Mar.     5 

5.30  P.M. 

I 

IO.O            41 

1.6 

ih.  rom. 

7U 

7300 

5<>57 

6 

2.00      " 

2 

5.0 

20 

0.5 

oh.  33m. 

170 

12  7OO 

5059 

"       6 

3-30      " 

2 

5.0 

20 

0-7 

2h.  03111. 

630 

29  500 

5060 

"       6 

5.00     " 

2 

5.0 

20 

0.9 

3h.  33m. 

1093 

24OOO 

3io 


W A TEK   PURIFICATION  A T  LOUISVILLE. 


RESULTS    OF     CHEMICAL     ANALYSES     OF     THE     OHIO     RIVER    WATER    BEFORE    AND     AFTER 
TREATMENT    BY    THE    MARK    AND    BROWNELL    DEVICES    AND    THE    JEWELL    FILTER. 

(Parts  per  Million.) 


1 
y. 

Collected. 
Date. 

,897. 

ga 

H 

C 

^ 

I 
O 

o 

Nitrogen 

0 

K 

aporat 

1 

Fixed  Residue 
after  Ignition. 

ft 

- 

•o 

c 

as  Albumin 

H 

s 
£ 

=  l 

z 

•a 

T: 

-, 

1 

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Decomposition  of  the  Browncll  Iron  Electrodes — 
Loss  of  Metal. 

During  the  period  covered  by  the  official 
tests  of  the  Brownell  electrodes  the  total 
quantity  of  water  treated  was  29  965  cubic 
feet;  the  duration  of  treatment  for  this  total 
quantity  of  water  was  33.25  hours,  and  the 
average  number  of  amperes  of  current  was  401. 
The  difference  in  the  weights  of  these  elec 
trodes,  at  the  beginning  and  at  the  end  of 
these  tests,  showed  a  loss  of  17.5  pounds.  This 
indicates  an  average  decomposition  of  0.59 
gram  (9.02  grains)  of  metallic  iron  per  am 
pere  hour.  Carefully  conducted  experiments 
made  on  a  small  scale  with  bright  iron,  free 
from  all  rust,  showed  that  the  rate  of  decom 
position  was  rather  variable,  but,  on  an  aver 
age,  it  approached  the  theoretical  rate  of  1.05 


grams  (16.17  grains)  per  ampere  hour.  These 
small  experiments  also  showed,  however,  that 
the  rate  of  decomposition  diminished  as  the 
electrodes  continued  in  service.  The  reason 
of  this  appeared  to  be  associated  with  coat 
ings  of  rust  on  the  surface  of  the  electrodes, 
especially  on  the  anode  (positive  pole).  It 
will  be  noted  that  in  these  official  tests  the 
actual  average  rate  of  decomposition  of  iron 
was  only  56  per  cent,  of  the  theoretical  rate. 
This  question  of  the  rate  of  the  electrolytical 
decomposition  of  metallic  iron  is  one  of  great 
practical  importance  in  this  connection,  be 
cause  it  is  a  controlling  factor  in  determining 
the  size  of  power  plant  which  would  be  re 
quired  in  the  application  of  this  process. 
Further  investigations  were  made  along  this 
line  after  the  close  of  the  work  on  the  Mark 
and  Brownell  devices,  and  the  results  are  re 
corded  in  Chapter  XV. 


THE  MARK  AND   BROWNELL   ELECTROLYT1CAL   DEVICES. 


Loss  of  Electrolytically  Formed  Hydrate  of  Iron 
in  the  Broii'iicll  Cell  due  to  the  Arrange 
ment  of  its  Outlet  Pipe. 

From  the  foregoing  description  of  the  elec 
trolytic  cell,  it  will  be  recalled  that  the  outlet 
water-pipe  was  not  placed  at  the  bottom  of 
the  cell,  but  at  the  side,  about  6  inches  above 
the  apex  of  the  conical  bottom.  The  portion 
of  the  cell  beneath  the  outlet  pipe  had  a  ca 
pacity  of  about  2.8  cubic  feet,  equal  to  21  gal 
lons.  At  Prof.  Brownell's  recommendation 
the  liquid  and  solid  materials  at  the  bottom  of 
the  cell  were  blown  into  the  sewer  about  once 
an  hour.  The  quantity  removed  each  time 
was  about  2  cubic  feet  on  an  average. 

It  was  very  soon  noticed  that  the  liquid, 
which  was  removed  in  this  way  from  time  to 
time,  subsided  very  quickly,  and  evidently 
contained  a  large  amount  of  iron  hydrate. 
On  Feb.  23,  when  the  river  water  was  very 
muddy  and  contained  4372  parts  per  million 
of  suspended  matter,  a  test  was  made  to  learn 
the  amount  of  iron  hydrate  which  passed  to 
the  sewer  through  the  blow-off  pipe. 

Samples  of  the  semi-liquid  matter,  which 
was  blown  off  into  a  cask  before  passing  to 
the  sewer,  were  carefully  collected  after  thor 
ough  mixing,  and  corresponding  samples  of 
the  untreated  river  water  were  also  taken. 
The  experiment  was  continued  during  the 
afternoon  of  this  day.  The  results  of  the 
analyses  of  the  several  samples  of  river  water 
and  blow-off  water,  respectively,  indicated 
that  the  iron  coming  from  the  electrodes  and 
leaving  the  cell  in  this  manner,  was  equiva 
lent  to  0.52  gram  (7.94  grains)  of  metallic  iron 
decomposed  per  ampere-hour  during  this 
test. 

It  is  impossible  to  state  accurately  what 
the  rate  of  decomposition  of  iron  was  during 
the  afternoon  of  Feb.  23,  but  it  is  probable 
that  it  was  not  far  from  the  average  rate  for 
all  the  runs,  as  stated  in  the  last  section.  This 
would  mean  that  84  per  cent,  of  the  iron 
which  came  from  the  electrodes  and  left  the 
cell,  passed  to  the  sewer  with  a  portion  of  the 
heaviest  mud,  before  there  was  an  opportun 
ity  for  it  to  coagulate  the  finer  particles  in 
the  water,  and  prepare  it  for  efficient  filtra 
tion.  Owing  to  the  very  muddy  condition  of 
the  river  water  on  this  date,  it  is  probable  that 


the  above  experiment  exaggerates  the  prac 
tical  significance  of  this  point,  with  reference 
to  ordinary  river  water.  Nevertheless,  it 
throws  much  light  on  the  actual  conditions 
at  that  time,  and  illustrates  a  weakness  in  the 
arrangement  of  the  cell. 

Passages  in  the  Cell  containing  the  Brownell 
Electrodes,  tliroitgh  which  the  River  IVater 
could  pass  with  little  or  no  direct  Elcctro- 
l\tical  Treatment. 

In  the  electrolytic  cell  containing  the 
Brownell  electrodes,  the  regular  spaces  be 
tween  the  electrodes  for  the  passage  of  the 
water  to  be  treated  were  0.5  inch.  There 
were  also  two  spaces  2  inches  in  width,  be 
tween  the  sections  in  which  the  plates  were 
arranged;  and  in  addition  to  this,  there  was 
an  annular  space,  ranging  from  3  to  3.5  inches 
in  width,  between  the  edge  of  the  electrodes 
and  the  wall  of  the  cell.  The  quantity  of  elec 
tric  current  which  can  pass  through  a  j-inch 
water  space  is  only  one-fourth  as  much  as 
can  pass  through  a  half-inch  water  space, 
other  conditions  being  equal;  and  there  was 
practically  no  current  passing  through  the  an 
nular  space  between  the  cell  and  the  electrodes. 
The  percentages  of  the  total  sectional  area  of 
the  cell  which  was  occupied  by  the  electrodes 
and  the  water  spaces,  respectively,  together 
with  the  percentages  which  the  treatment  of 
the  water  passing  through  each  of  the  sec 
tions  was  of  the  maximum,  are  as  follows: 


These  figures  show  that,  originally,  there 
was  an  opportunity  for  fully  one-half  of  the 
water  to  pass  through  the  cell  without  direct 
electrolytic  treatment. 

On  Feb.  26,  an  annular  wooden  frame,  3 
inches  wide,  was  placed  in  the  cell  at  both 
the  top  and  the  bottom  of  the  electrodes,  and 
which  reduced  the  outer  annular  water  space, 
in  which  there  was  no  treatment,  from  31  to 
about  6  per  cent,  of  the  total  sectional  area 
of  the  cell.  This  corrected  in  part  the  defect 
of  having  some  of  the  water  pass  through  the 
cell  without  coming  at  once  in  intimate  con 
tact  with  the  coagulant  during  its  initial  for- 


312 


WATER   PURIFICATION  AT  LOUISVILLE. 


mation.  All  the  official  rims  with  this  cell, 
however,  were  made  before  the  frames  were 
put  in  place.  But  on  the  following  day  the 
cell  was  used  in  its  modified  form,  on  an  un 
official  run,  and  the  devices  failed  to  purify  the 
water  satisfactorily. 

With  the  conditions  which  would  be  ob 
tained  upon  a  large  scale  of  operation,  it  is 
very  probable  that  this  defect  in  the  arrange 
ment  of  the  cell  would  reduce  the  efficiency 
of  the  treatment,  owing  to  the  lack  of  uniform 
distribution  of  the  solid  hydrate  in  the  water. 
In  this  experimental  cell,  however,  it  is  doubt 
ful  whether  the  point  in  question  exerted  any 
influence,  because  the  piping  was  so  arranged 
that  after  leaving  the  cell,  the  water  passed 
through  several  elbows,  valves,  and  meters, 
all  of  which  aided  in  mixing  well  together  the 
treated  and  untreated  portions  of  the  water. 

Variations  in  the  Resistance  of  Ohio  River  Water 
to  the  Passage  of  an  Electric  Current. 

As  already  stated  in  the  description  on  the 
operation  of  these  devices,  it  was  found  that 
up  to,  and  including,  Feb.  24,  it  was  possible 
to  pass,  for  a  short  time,  500  amperes  of  cur 
rent  at  a  potential  of  40  volts  through  the 
cell  containing  the  Brownell  electrodes.  But 
on  several  days  following  this  date  the  maxi 
mum  potential  (55  volts)  of  the  dynamo 
could  give  only  about  375  amperes.  On  ac 
count  of  the  fact  that  it  is  the  amperage  of 
the  current  which  controls  the  amount  of 
electrolytic  decomposition,  this  reduction  of 
about  45  per  cent,  in  the  efficiency  of  the 
plant,  with  substantially  the  same  expenditure 
of  power,  is  a  very  serious  problem  from  a 
practical  point  of  view.  Considerable  study 
was  given  to  the  matter,  and  it  was  found  that 
it  was  caused  during  this  flood  by  the  dilution 
of  the  dissolved  chemical  compounds  in  the 
river  water.  So  far  as  could  be  learned,  the 
mud  and  other  suspended  matters  in  the  river 
water  exerted  practically  no  influence  on  its 
conductivity.  That  is  to  say,  with  small  elec 
trodes  placed  in  two-gallon  jars,  it  apparently 
made  no  difference  in  the  resistance  of  the 
same  river  water,  whether  the  suspended  mat 
ters  were  present  or  whether  they  were  re 
moved  by  the  passage  of  the  water  through 
filter  paper  or  a  Pasteur  filter.  The  results 


of  further  studies  along  this  line  are  recorded 
and  discussed  in  Chapter  XV. 

In  the  following  table  are  presented  com 
parative  results,  showing  the  specific  re 
sistance  of  the  Ohio  River  water,  expressed 
in  the  conventional  form,  during  the  period 
of  flood  from  Feb.  22  to  March  6.  They 
serve  to  show  the  variations  which  were  en 
countered  in  the  river  water;  and  they  also 
indicate  the  range  in  power  which  would  be 
required  to  do  the  same  amount  of  efficient 
work,  other  thing's  being  equal.  As  will  be 
seen  by  the  comparison  of  these  results  with 
small  electrodes  (150  centimeters  square)  with 
the  results  referred  to  in  Chapter  XV,  and 
which  were  obtained  from  the  use  of  large 
electrodes,  these  figures  can  be  safely  used  in 
estimating  the  required  amount  of  electro 
motive  force  for  different  services  in  which 
the  Ohio  River  water  is  used  as  an  electro 
lyte. 

SPECIFIC  RESISTANCE  OF  THE  OHIO  RIVER 
WATER,  EXPRESSED  IN  OHMS  PER  CENTI 
METER  CUBE. 


Number  of  Correspond 
ing  Chemical  Sample.* 

Date. 

1897. 

Specific  Resistance. 

835 

February  22 

7  300 

837 

23 

5  9°° 

839 

24 

8  700 

841 

25 

II  600 

842 

26 

13  200 

843 

27 

16  700 

844 

March        I 

12  300 

845 

2 

14900 

846 

3 

11  250 

847 

4 

14  ooo 

848 

5 

7900 

850 

6 

7  200 

*  The  chemical  composition  of  these  samples  may  be  seen 
by  reference  to  Chapter  I. 


In  the  foregoing  summary  of  results,  the 
electric  horse-power  used  during  each  run  is 
given.  The  relation  between  the  electric 
power  and  the  actual  steam  power  used,  both 
with  regard  to  these  conditions  and  the  prac 
tical  conditions  on  a  large  scale,  are  discussed 
in  Chapter  XV.  As  a  more  accurate  idea  of 
the  cost  of  generating  electric  power,  it  may 
be  stated  here,  that  these  generating  appli 
ances,  under  the  most  favorable  conditions, 
yielded  about  80  per  cent,  of  the  power  con- 


THE  MARK  AND   BROW  NELL   ELECTROLYTICAL   DEVICES. 


tained  in  the  steam  which  was  used.  On  a 
large  scale  it  may  be  reasonably  expected  that 
this  efficiency  could  be  maintained  or  slightly 
increased. 

General  Status  of  this  1'rocess  at  the  Close  of 
these  Tests. 

A . — Broivndl  Electrodes. 
The  summary  of  analytical  results  obtained 
in  connection  with  the  Brownell  electrodes, 
already  presented,  shows  that  at  no  time  was 
the  filtered  water  satisfactory,  either  with  re 
gard  to  appearance  or  to  the  number  of  bac 
teria  contained  in  it.  The  amount  of  organic 
matter  in  the  filtered  water,  as  indicated  by 
the  nitrogen  in  the  form  of  albuminoid  am 
monia,  and  by  the  oxygen  consumed,  was 
several  times  as  great  as  was  normally  present 
in  the  filtered  water  during  the  previous  year. 
Owing  to  the  very  muddy  condition  of  the 
river  water,  however,  and  the  consequently 
large  amount  of  organic  matter  which  it  con 
tained,  the  percentages  of  removal  of  organic 
matter  were  high. 

B. — Mark  Electrodes. 

The  Mark  electrodes,  composed  of  circular 
cast-iron  pipes,  were  placed  in  a  duplicate 
cell,  and  were  used  in  connection  with  the 
same  generating  appliances  as  in  the  case  of 
the  Brownell  electrodes,  for  two  runs,  which 
were  made  on  March  5  and  6,  respectively. 

At  this  period  the  river  water  was  very 
muddy,  and  on  March  6  it  was  in  the  mud 
diest  condition  which  existed  during  the  en 
tire  investigations.  Very  little  information 
wras  obtained  from  the  results  of  these  two 
tests,  other  than  that  the  filtered  water  was 
muddy,  showing  that  the  devices  were  wholly 
inadequate  to  coagulate  the  water  properly, 
even  at  one-fifth  of  the  regular  rate  of  treat 
ment  and  of  filtration. 

Considering  these  electrodes  in  general 
terms,  however,  they  seemed  to  possess  some 
advantages  over  the  Brownell  electrodes  in 
arrangement  for  operation  on  a  large  scale,  in 
that  the  water  was  uniformly  treated.  I>ut 
in  these  experimental  cells,  the  outlet  pipe 
leading  to  the  Jewell  settling  chamber  was  so 
arranged  that  it  is  doubtful  whether  any  such 
advantage  existed  here.  It  is  also  possible 
that  the  cost  of  construction  of  complete  sets 


of  electrodes  on  a  large  scale  would  be  less 
in  the  case  of  the  Mark  electrodes.  These 
latter  electrodes  possessed  a  disadvantage 
when  compared  with  the  former,  in  that  the 
water  space  between  the  individual  electrodes 
was  twice  as  great,  and,  accordingly,  the 
amount  of  power  required  would  be  twice  as 
great,  other  things  being  equal. 

It  seems  hardly  necessary  to  state  that 
these  poor  results  were  caused  by  inadequate 
preparation  of  the  river  water  before  its  pas 
sage  through  the  Jewell  filter;  and,  further, 
that  in  the  absence  of  sufficient  coagulation 
these  results  cannot  be  taken  as  a  measure  of 
the  merits  and  practicability  of  the  general 
method  of  water  purification,  in  which  the 
electrolytic  treatment  is  a  preliminary  step 
preceding  filtration.  These  results  refer  only 
to  a  particular  set  of  devices,  possessing  a 
number  of  weaknesses,  which  might  be 
remedied  in  a  large  measure  by  practical 
means. 

In  this  connection,  it  must  not  be  over 
looked  that,  as  already  stated,  the  electrolytic 
treatment  of  water  adds  to  it  no  sulphuric  acid 
to  combine  with  lime  and  form  incrustations 
in  steam  boilers;  nor  does  it  liberate  in  the 
water  carbonic  acid  gas  to  increase  the  cor 
roding  action  of  the  water  on  wrought-iron 
receptacles.  This  advantage  of  the  electro 
lytic  formation  of  coagulating  chemicals 
(either  aluminum  hydrate  or  iron  hydrate), 
over  the  decomposition  of  the  commercial 
sulphates  of  these  metals  by  the  lime  dissolved 
in  the  water,  is  a  matter  of  importance.  An 
other  advantage  of  the  electrolytic  treatment 
is  that  it  is  independent  of  the  amount  of  lime 
dissolved  in  the  river  water,  and  the  possibil 
ity  of  undecomposed  sulphates  passing  into 
the  filtered  water  is  obviated.  A  further  con 
sideration  of  this  process  in  its  various  phases 
will  be  found  in  Chapter  XV. 

COMPARISON  OF  THE  QUALITY  OF  TIIK  OHIO 
RIVF.R  WATER  AFTER  FILTRATION  FOL 
LOWING  ELECTROLYTIC  TREATMENT  IN 
THE  BROWNELL  CELL,  AND  AFTER  FiL- 
TUATlOX  WITHOUT  ANY  PRELIMINARY 
TREATMENT. 

As  requested  by  President  Long,  two  runs 
were  made  with  the  Jewell  filter  on  March  i  i . 
The  first  run  was  made  at  the  regular  rate  of 


WATER  PURIFICATION  AT  LOUISVILLE. 


23.5  cubic  feet  per  minute,  and  the  river  water 
before  filtration  was  treated  with  the  maxi 
mum  electric  current  (400  amperes)  in  the 
Brownel!  electrolytic  cell.  The  second  run 
was  made  at  the  same  rate,  but  the  river  water 
received  no  preliminary  coagulating  treat 
ment  whatever.  In  each  case  the  settling 
basin  of  the  Jewell  System  was  drained  and 
cleaned,  and  the  filter  thoroughly  washed  be 
fore  filtration  was  begun.  Both  runs  were 
continued  until  the  filter  became  clogged  so 
that  it  would  not  allow  the  passage  of  water 
at  the  prescribed  rate. 


A  comparison  of  the  result  obtained  from 
these  two  runs  is  shown  in  the  following 
table: 

BACTERIA  PER  CUBIC  CENTIMETER  IN  THE 
OHIO  RIVER  WATER  TREATED  DURING  THE 
COMPARATIVE  TESTS  DESCRIBED  ABOVE. 


*  Sample" 

Date. 

Hou, 

Bacteria  per  Cubic 

1897 

5081 

March  11 

9.30  A.M. 

38  IOO 

508.) 

"       ii 

1.  00   P.M. 

41  500 

5087 

"       ii 

3-25      " 

36  2OO 

COMPARATIVE  SUMMARY  OF  RESULTS  ACCOMPLISHED  BY  THE  JEWELL  FILTER  WITH  (RUN  NO.  i) 
AND  WITHOUT  (RUN  NO.  2)  PRELIMINARY  TREATMENT  BY  THE  MARK  AND  BROWNELL 
DEVICES.  (Brownell  Electrodes.) 


Bej 

an. 

••Electric 

Current. 

Quantities 
'       Cubic 

of  Water. 
Feet. 

Average 
Filtr 

Rates  of 

Mum  her 
of  Run. 

H.P.  per 
Million 

Ampere 

Million 

Service. 
Hours  and 

1897. 

Gallons  per 
24  Hours. 

Gallon. 

per  Minute. 

A  Hour"  *4 

March  n 

85 

80 

Estimated 
Average 

Suspended 

Solids  in 

Oelrness! 

Nitro^as 

Albumino 
ts  per  Mill 

dA—onta. 

% 

gen  Consul 
ts  per  Mill 

ned. 

Average  E 
Cubic  C 

acteria  per 

River  Water. 
Parts  per 
Million. 

Effluent. 

River  Water. 

Effluent. 

Per  Cent. 

Removed. 

River  Water. 

Effluent. 

Per  Cent. 
Removed. 

River  Water. 

Effluent. 

I  751 
I  751 

Muddy. 

2.400 
2.400 

-374 
.566 

34 
76 

24.6 
24.6 

6-4 
9.0 

74 
63 

39800 
36  20O 

13  IOO 
2O  2OO 

67.0- 
44.0 


NUMBER    OF    BACTERIA    IN    THE    EFFLUENT    OF    THE    JEWELL    FILTER     WITH    AND    WITHOUT 

ELECTROLYTIC    TREATMENT. 


Rate  of 

!    8* 

8         ! 

Collected. 

Filtration. 

£ 

•jj 

15 

i 

Number 

S. 

i& 

,,- 

Period  of 
ServiceSince 

t  c    . 

u  u. 

s 

of 
Run. 

C  . 

•5£|» 

1 

Washing. 

^1l 

Is 

Remarks. 

X 

Date. 

'j-    - 

"^  o 

^- 

Hours  and 

T3  ^   o            ,5-S 

1897. 

Hour. 

u  c 

o  UX 

° 

Minutes. 

^  «  •£      i;  c 

•c 

Is 

38.? 

0 

^  JU 

0(J 

Ji 

o 

s 

J 

£ 

CO 

Effluent    with    Electrolytic    Treatment. 

5082 

March  n 

12.50  I'.M. 

I 

23-5 

95 

IO.O 

oh.  55m. 

i  287 

12  7OO 

5083 

"        ii 

I.OO      " 

I 

23-5 

95 

10.8 

ih.  osm. 

i  5i7 

13500 

Effluent   with    No   Coagulating   Treatment. 

5085        March   n                3.15  I'.M. 

2 

23.0 

93 

5.6 

ih.  02m. 

1386 

17700 

5086 

ii 

3-25     " 

2 

23.0 

93 

7-9 

ih.  I2tn. 

i  636 

19  700 

5088 

"       ii 

3-55    " 

2 

23.0 

93 

II.  O 

ill.  42111. 

•2  197 

23  2OO 

THE  MARK   AND  BROWN  ELL   ELECTROLYTICAL   DEVICES. 


3'5 


RESULTS  OF  CHEMICAL  ANALYSES  OF  THE  OHIO  RIVER  WATER  BEFORE  AND  AFTER 
FILTRATION  THROUGH  THE  JEWELL  FILTER  WITH  AND  WITHOUT  ELECTROLYTIC 
TREATMENT. 

(Parts  per  Million.) 


;• 

•a 

Nitrogen 

Residue 

90 

Fixed  Residue 

. 

U 

:: 

B 

3 

as 

« 

Rvaporat 

'"' 

alter  Ignition. 

i 

£ 

a  P 

0 

g 

Ammonia. 

i 

« 

d 

•u 

•6 

< 

Corresponding 

r!  M 

o 

-.  B 

«'^ 

1   d 

V 

•D 

_ 

E 

.- 

* 

Date. 

Bacterial  Num. 

aa 

tj 

s 

u 

< 

.- 

- 

j 

j£ 

c 

JJ 

.£ 

** 

.2 

.897. 

bers  or  Hour  of 

B 

•-, 

>, 

2 

i  = 

,  -| 

i! 

z 

5 

a 

, 

2 

1 

! 

0! 

, 

c 

y, 

S- 

Q 

. 

o 

f- 

3  a 

Q 

£ 

U 

H 

1 

a 

h 

3 

la 

< 

Q 

~ 

ssi1 

Mar.  ii 

9.30  A.M. 

II.O 

.22 

24.6 

2.400 

2.274 

.126 

.042 

.002 

:  .  I 

5-1 

1881 

1751 

I  )0 

1766 

1664 

102 

61.0 

O 

96.0 

8s6-j 

"     1  1 

5082,  5083 

II.  O 

5 

6.4 

•374 

.248 

.126 

•  036 

.003  1  i 

5-0 

587 

547  I3°!  537 

435 

102  60.7 

O 

21.0 

«57" 

"     ii 

5085,   5086 

II.  0 

5 

9.0 

5.66 

.440 

.126 

.034 

.005 

1-3 

5  '^ 

763 

633 

130  704 

602 

IC2 

03.1 

O 

28.0 

A  COMPARISON  OF  THE  EFFICIENCY  IN  THE 
ELECTROLYTIC  TREATMENT  OF  WATER 
BEFORE  FILTRATION,  OF  THE  BROWNELL 
ELECTRODES  AND  OF  ALUMINUM  ELEC 
TRODES  OF  THE  SAME  SlZE  AND  AR 
RANGEMENT. 

At  President  Long's  request,  a  set  of  alu 
minum  electrodes  was  made  to  duplicate  as 
nearly  as  possible  the  iron  electrodes  devised 
by  Prof.  Brownell.  Owing  to  delays  in  secur 
ing  the  aluminum  plates,  it  was  not  until 
April  2  that  these  comparative  tests  could  be 
made.  These  aluminum  electrodes  were 
placed  in  the  cell  which  formerly  contained 
the  Mark  electrodes.  From  April  2,  at 
3.41  P.M.,  to  April  4,  at  6.30  A.M.,  nine  runs 
were  made  in  connection  with  the  Jewell  Sys 
tem.  The  first  five  were  made  with  the  iron 
(Brownell)  electrodes,  and  in  the  last  four 
runs  the  aluminum  electrodes  were  used.  The 
rate  of  treatment  and  filtration  was  kept  as 
nearly  as  possible  to  the  regular  rate  of  23.5 
cubic  feet  per  minute,  and  the  conditions  of 
operation,  other  than  the  amount  of  current 
used,  were  as  nearly  the  same  as  possible.  In 
the  case  of  each  cell,  no  sediment  was  blown 
off  at  the  bottom. 

It  was  found  that  a  current  of  100  amperes 
on  the  aluminum  electrodes  was  sufficient  to 


secure  a  perfectly  clear  effluent,  while  with 
450  amperes  of  current  on  the  iron  electrodes 
the  effluent  was  not  clear.  The  iron  elec 
trodes,  however,  were  somewhat  covered  with 
rust  from  their  earlier  use,  while  the  alu 
minum  electrodes  were  new  and  bright.  It 
was  found  that  the  iron  electrodes,  following 
the  long  period  of  disuse,  gave  more  efficient 
coagulation  as  they  continued  in  service. 
\Yhile  these  experiments  were  continued  suf 
ficiently  to  serve  their  general  purpose,  yet 
they  were  of  too  short  duration  to  allow  satis 
factory  determinations  of  the  amount  of  metal 
used,  owing  to  complications  from  mud, 
rust  and  water.  The  principal  data  of  these 
comparative  tests  are  presented  in  the  follow 
ing  summary  and  results  of  analyses: 

BACTERIA  I>ER  CUHIC  CENTIMETER  IN  THE 
OHIO  RIVER  WATER  TREATED  DURING  THE 
COMPARATIVE  TESTS  DESCRIBED  ABOVE. 


Serial 
Number. 

Date. 

1897. 

Hour. 

Bacteria  per 
Cubic  Centimett 

5226 

April  2 

5.30  P.M. 

3  700 

5228 

2 

8.00      " 

3420 

5230 

3 

12.30  A.M. 

2940 

5232 

3 

3-30       " 

3500 

5234 

3 

9.30       " 

3  150 

5243 

3 

3.30  P.M. 

4  200 

5249 

3 

9.30      " 

6  400 

5252 

4 

12.30  A.M. 

5  100 

5259 

4 

5.30      " 

5  7oo 

3i6 


WATER   PURIFICATION   AT  LOUISVILLE. 


COMPARATIVE  SUMMARY  OF  RESULTS  ACCOMPLISHED  BY  THE  JEWELL  FILTER  AND  MARK 
AND  BROWNELL  DEVICES  WITH  IRON  ELECTRODES  (RUNS  NOS.  1  TO  5)  AND  ALUMINUM 
ELECTRODES  (RUNS  NOS.  6  TO  9). 


Began. 

Electric  Current. 

Quantities  of  Water. 
~       Cubic  Feet. 

Average  Rates  of  Filtration. 

Periods  of 

of  Run. 

H   P  per 

Cubic  Feet 

Million  Gallons 

Hours  and 

Date. 

1897. 

Hour. 

Million  Gallons 
per  24  Hours. 

per  Gallon. 

Filtered. 

Wash. 

per 
Minute. 

per  Acre  per 

I 

April  2 

4.28  P.M. 

95 

0.047 

5  214 

518 

23-5 

95 

3h.  42m. 

2 

"     •> 

8.33      " 

78 

0.042 

7265 

603 

23.6 

95 

5h.  o8m. 

3 

"     3 

2.07  A.M. 

65 

0.041 

5902 

602 

21.  8 

88 

4h.  3im. 

4 

"     3 

7.07       ' 

35 

0.029 

4970 

568 

23.2 

94 

3h.  34m. 

6 

"     3 

3.36  P.M. 

24 

0.024 

4092 

514 

23.2 

94 

2h.  55m. 

7 

"     3 

6.57     " 

20 

O.O2O 

4552 

541 

22.5 

91 

3h.  2301. 

9 

"     4 

2.44  A.M. 

6 

O.OO8 

4974 

21  .2 

86 

3h.  54m. 

£  . 

Estimated 
Average  Sus- 

Degree  of 

Nitrogen  as  Albuminoid  Ammonia. 
Parts  per  Million. 

Oxygen  Consumed. 
Parts  per  Million. 

Average  Bacteria 
per  Cubic  Centimeter. 

Average 

Bat 
z 

in  River  Water- 
Parts  per  Million. 

of 

Effluent. 

River 
Water. 

Effluent. 

Per  Cent. 
Removed. 

River 
Water. 

Effluent. 

Per  Cent. 
Removed. 

River 
Water. 

Effluent. 

Efficiency. 

i 

213 

3 

.248 

•075 

71 

4-5 

.2 

73 

3300 

3" 

90.4 

2 

213 

.248 

•  075 

71 

4-5 

.1 

76 

2  900 

133 

93-3 

3 

213 

3 

.248 

.075 

7' 

4-5 

.0 

78 

3500 

154 

95.6 

4 

213 

3 

.248 

.075 

71 

4-5 

.  I 

76 

3  Io° 

240 

92-3 

5 

200 

3 

.248 

."75 

71 

4-5 

.0 

78 

3700 

207 

94-4 

6 

200 

i 

.208 

.050 

76 

4.8 

o.S                83 

5300 

94 

98.2 

7 

2OO 

i 

.208 

.050 

76 

4.8 

o.S                83 

5700 

IOO 

98.2 

8 

2OO 

i 

.208 

.050 

76 

4.8 

0.8 

83 

5700 

126 

97.8 

9 

2OO 

i 

.208 

•  050 

76 

4.8 

0.9 

Si 

5400 

138 

97.6 

RESULTS  OF  CHEMICAL  ANALYSES  OF  THE  OHIO  RIVER  WATER  BEFORE  AND  AFTER  TREAT 
MENT  BY  THE  MARK  AND  BROWNELL  DEVICES  AND  THE  JEWELL  FILTER  WITH  IRON 
ELECTRODES  AND  ALUMINUM  ELECTRODES,  RESPECTIVELY. 

(Parts  per  Million.) 


Collected. 

\ 

i 

Nitrogen 

Residue  on 
Evaporation. 

Fixed 
Residue  after 
Ignition. 

£ 

£ 
a 

i 

J3 

g 

S£     u 

c 

e 

£ 

8 

..; 

— 

<-• 

3 

Corresponding 

o 

•:                                 • 

. 

«  'C 

',  , 

', 

-.; 

91 

-_: 

V 

S 

Date. 

£   t£         0 

• 

i        aj 

U 

< 

.ti 

- 

.£ 

s 

•' 

8 

Jfc 

5 

£ 

73 

1897. 

Hour  of  Collection. 

IQ 

si 

•- 

;.' 

2      Ji  £     i"3 

0 

. 

~ 

a 

; 

3 

t. 

1 

| 

| 

<J! 

H 

Q 

u 

o 

H 

«a  P 

b. 

U 

- 

•'• 

Q 

- 

•/; 

5 

< 

a 

River  Water. 

875 

Apr.  2,  3 

5.30  P.M.,    8.00  P.M. 
12.  30  A.M.,    9.30A.M. 

10.5 

.16 

4-5 

.248 

.166 

.082 

.O2O 

.OO2 

1.2 

4-5 

"2? 

213 

112 

229 

2O9 

9° 

39-2 

o 

8.8 

878 

"     3,4- 

3.30  P.M.,    9.30  P.M. 
12.  30  A.M.,    5.  30  A.M. 

II.  0 

.20 

4.8 

.208 

.138 

.070 

.014 

.OOI 

0.8 

2.8 

3°« 

200 

IO9 

2Si|i93 

88 

43.8    o 

12.8 

Effluent  with 

Iron   Electr 

odes 

i. 

rr> 

TOI 

0 

' 

3 

Tfi 

0« 

.) 

T3 

93 

o 

J 

96 

o 

876 

877 

"     2,  3 

"     3 

5227,5229,5231,  5233 
5235,   5241 

II  .0 

3 

3 

.32 
.20 

.2 
.O 

.076 
.074 

.014 
.016 

.001 

.000 

I.O 

0.9 

3-o 
3-° 

12 

08 

93 
92 

'.'.'. 

42.0 
42.0 

o 
o 

I  .0 

0.5 

Effluent  with  Aluminum   Electrodes. 

879a 
879b 
8790 

8791! 
879 

Apr.  3 
"     3 
"     4 
"     4 
"     3,  4 

5=45 
5247 
5253 
5258 
5245,5247,5253,  5258 

11.4 

06 

90 

o 

... 

o  8 

"  1 

«7 

0 

... 

no 

85 

(1 

06 

84 

0 

.IO 

0.8 

.050 

.000 

.050 

.016 

.002 

i-3 

2.9 

03 

o 

l<>3 

83 

0 

8344.1 

o.o 

THE  MARK  AND   BROWN  ELL   ELECTROLYTICAL    DEVICES. 


NUMBER  OF  BACTERIA  IN  THE  EFFLUENT  OF  THE  JEWELL  FILTER  FOLLOWING  TREAT 
MENT  IN  THE  MARK  AND  BROWNELL  DEVICES  WITH  IRON  ELECTRODES  AND  ALUMINUM 
ELECTRODES,  RESPECTIVELY. 


Rate  of 

S 

«j 

Collected. 

Filtration. 

£ 

c 

•J 

3 

Number 

S. 

1*. 

i 

Period  of 
Service  Since 
Last 

aj  c    . 

u  ^ 

S 

3 

Date. 

1897. 

Hour. 

Run. 

k  = 

O  u  3 

•3 

Washing. 
Hours  and 
Minutes. 

|f| 

rt  a 

Remarks. 

u 

•fsi 

~  D.  cT 

i 

—  *JCJ 

rt  ^ 

en 

(J 

s 

2 

£ 

K 

Effluent  with    Iron   Electrodes. 

5227 

April  2 

5.30  P.M. 

I 

24.0         97 

3-5 

ih.  O2m. 

1499 

385 

522O 

8.00     " 

I 

24.  o 

97 

3h.  32m. 

250 

5231 

"     3 

12.30  A.M. 

2 

24.0 

97 

7-3 

3h.  57m. 

5  555 

193 

5233 

"     3 

3.30      " 

3 

24.0 

97 

3-9 

ih.  23m. 

i  710 

154 

5235 

'     3                    9.30     " 

4 

23-5 

95 

5-3 

2h.  23m. 

3378 

267 

5236 

'     3                  10.00     " 

4 

23-5 

95 

7-5 

2h.  53m. 

4088 

239 

5237 

"     3                 10.30     " 

4 

22.0 

89 

9-7 

3h.  23m. 

4768 

214 

5238 

"       3                         12.  OO  M. 

5 

23-5 

95 

3-5 

oh.  48m. 

i  148 

219 

5239 

"     3                   12.30  P.M. 

5 

23-5 

95 

3-9 

ih.  iSm. 

i  868 

198 

5240 

"     3                     i.  oo     " 

5 

23.5 

95 

4-3 

ih.  48m. 

2538 

181 

5241 

"3                     1.30     " 

5 

23-5 

95 

5.3      2h.  iSm. 

3  208 

222 

5242 

"     3                     2.00     " 

5 

20.0 

Si 

8.6 

2h.  4Sm. 

3928 

217 

Effluent  with   Aluminum    Electrodes. 

5244 

April  3 

4.0O  P.M. 

6 

24.0 

97 

3-1 

oh.  24m. 

588 

107 

5245 

"     3 

4.30      " 

6 

23.0 

93 

3-4 

oh.  54m. 

i  238 

85 

5246 

"     3 

5.30      " 

6 

23.5 

95 

5-7 

ih.  54m. 

2  7lS 

91 

5247 

"     3 

8.00     " 

7 

23-5 

95 

3-8 

ih.  03111. 

I  594 

106 

5248 

"     3 

9.00     " 

7 

23-5 

95 

5  7 

2h.  03m. 

2976 

95 

5250 

"     3 

10.00     " 

7 

23-5 

95 

10.9 

3h.  03111. 

4306 

120 

5251 

'  '     3 

11.30     " 

8 

23-5 

95 

3.0 

oh.  45m. 

1074 

159 

5253 

"     4 

12.30  A.M, 

8 

23.5 

95 

4.0 

ih.  45m. 

2474 

no 

5254 

"     4 

1.30      " 

8 

23.5 

95 

7.0 

2h.  45m. 

3834 

I  1O 

5255 

"     4 

2.0O       " 

8 

23.0 

93 

9.8 

3h.  ism. 

4544 

139 

5256 

"     4 

3-30       " 

9 

23-5 

95 

oh.  4601. 

812 

199 

5257 

"     4 

4.30       " 

9 

23-5 

95 

3-9 

ih.  46m. 

2342 

93  i 

5258 

"     4 

5.30       " 

9 

23-5 

95 

6.5 

2h.  46111. 

3692 

121 

WATER   PURIFICATION  AT  LOUISVILLE. 


CHAPTER   XIV. 

DESCRIPTION  OF  THE  MACDOUGALL  POLAR ITE  SYSTEM  OF  PURIFICATION, AND  A  RECORD 
OF  THE  RESULTS  ACCOMPLISHED  THEREWITH. 


ON  March  3,  1897,  just  as  the  tests  of  the 
Mark  and  Brownell  devices  were  being  com 
pleted,  arrangements  were  made  whereby  trie 
efficiency  and  cost  of  operation  of  the  Mac- 
Dougall  Polarite  System  should  be  investi 
gated,  with  reference  to  the  purification  of 
the  water  supply  of  this  Company.  In  order 
that  the  results  accomplished  by  this  system 
might  be  comparable  with  those  of  the  fore 
going  tests,  the  rate  of  treatment  was  ar 
ranged  to  be  250,000  gallons  per  24  hours. 

In  brief,  this  system,  known  abroad  both  as 
the  International  System  and  the  Howatson 
System,  was  represented  to  consist  of  a  double 
nitration  of  river  water,  without  the  use  of 
coagulating  chemicals,  obtained  either  elec- 
trolytically  or  from  commercial  chemical 
products.  The  first  filtration  was  to  be 
through  a  layer  of  sand,  with  the  view  to  re 
moving  the  coarser  matters  suspended  in  the 
river  water;  and  the  second  filtration  was  to 
be  through  a  layer  of  a  special  material,  called 
polarite,  which  is  described  below.  This  sys 
tem  of  water  purification  has  never  been  tried 
in  this  country,  but  it  is  said  to  be  in  success 
ful  operation  in  purifying  turbid  or  muddy 
waters  in  several  places  in  England,  Egypt, 
and  India. 

In  order  to  guard  against  delays,  it  was 
mutually  agreed  that  for  the  first  (sand)  filter 
use  should  be  made  in  an  undisturbed  condi 
tion  of  the  Jewell  filter,  which  was  then  at  the 
disposal  of  the  Water  Company.  Owing  to 
the  fact  that  it  was  necessary  to  send  to  Eng 
land  for  the  polarite,  this  system,  however, 
was  not  ready  to  be  tested  until  May  10. 

With  the  exception  of  Sundays,  and  sev 
eral  unavoidable  periods  of  delay,  this  system 
was  operated  night  and  day  from  May  10  to 
June  12,  inclusive.  During  the  remaining 


time,  from  the  close  of  the  tests  of  the  Mark 
and  Brownell  devices  until  the  end  of  the  in 
vestigations,  attention  was  directed  to  some 
plans  and  devices  of  the  Water  Company,  as 
are  described  in  Chapter  XV. 

When  the  MacDougall  Polarite  System 
was  being  constructed,  it  was  found  that  a 
separate  tank  with  baffle  plates  was  to  be  sub 
stituted  for  the  settling  basin  under  the  Jewell 
filter.  On  May  28,  a  "  clay  extractor,"  con 
sisting  of  an  iron  tank  with  two  compart 
ments,  each  filled  with  about  14  feet  in  depth 
of  coarse  coke,  was  substituted  for  this  tank 
containing  baffle  plates.  The  settling  basin 
and  filter  of  the  Jewell  System  have  been  fully 
described  in  the  foregoing  chapters,  and  a 
plan  and  section  have  also  been  presented.  A 
correct  understanding  of  the  other  devices 
used  in  connection  with  the  polarite  system 
may  be  obtained  from  the  following  descrip 
tion.  Meters  and  gauges  were  provided 
wherever  necessary,  in  order  to  secure  meas 
urements  of  the  quantities  of  water  which 
were  treated,  and  also  of  the  resistance  which 
the  water  met  as  it  passed  through  the  several 
layers  of  filtering  material. 

IRON  TANK  WITH  BAFFLE  PLATES. 

This  tank,  placed  just  outside  of  the  Jewell 
house,  was  cylindrical  in  form,  3  feet  in  di 
ameter,  16  feet  high,  113  cubic  feet  in  capac 
ity  and  made  of  boiler  iron,  0.19  inch  in 
thickness.  It  was  put  together  with  o.5-inch 
rivets.  The  bottom  of  the  tank  was  conical 
in  form,  2  feet  high  and  tapered  at  the  lowest 
point  to  an  apex  3  inches  in  diameter,  where 
a  blow-off  pipe  leading  to  the  sewer  was  con 
nected.  The  inlet  pipe,  leading  from  the  river 
water  main,  was  4  inches  in  diameter,  and  en- 


THE  MACDOUGALL   FOLAR1TE  SYSTEM   OF  PURIFICATION. 


tercel  the  tank  by  a  flanged  joint  about  5.5 
inches  above  the  point  where  the  conical  bot 
tom  with  a  shoulder  was  riveted  to  the  main 
cylinder.  In  this  main  cylinder  were  six  baffle 
plates,  placed  at  0.25,  2.25,  4.25,  6.25,  8.25 
and  10.25  feet,  respectively,  from  the  center 
of  the  inlet  pipe.  These  baffle  plates  were 
circular  in  form,  and  riveted  to  the  shell  of 
the  tank.  In  order  to  provide  a  passage  for 
the  water,  a  small  segment  of  each  plate  was 
cut  away,  leaving  a  maximum  perpendicular 
distance  between  the  edge  of  the  plates  and 
the  adjoining  shell,  of  about  4  inches.  The 
lowest  plate  was  cut  away  on  the  side  diam 
etrically  opposite  the  point  where  the  inlet 
pipe  entered;  and  the  openings  through  the 
remaining  baffle  plates  were  arranged  alter 
nately  with  reference  to  the  inlet  pipe  and  the 
opening  in  the  first  plate.  Perpendicular  to 
the  upper  baffle  plate,  which  was  3  feet  from 
the  top  of  the  tank,  two  iron  plates  were 
riveted  to  the  baffle  plate  and  to  the  shell  of 
the  tank.  Each  of  these  partition  plates  ex 
tended  to  within  12  inches  of  the  top  of  the 
tank,  and  they  were  each  22  inches  in  length. 
In  the  center  of  the  tank,  and  parallel  to  these 
two  partitions,  which  were  in  the  same  verti 
cal  plane  as  the  cut  edge  of  the  lower  baffle 
plate,  was  another  partition,  2.83  feet  in 
height,  extending  from  the  top  of  the  tank  to 
within  14  inches  of  the  upper  baffle  plate. 
Across  the  bottom  of  this  central  partition, 
and  extending  to  the  two  outer  partitions, 
was  a  false  bottom,  made  of  a  screen  with 
meshes  of  about  0.25  linear  inch.  In  the  inner 
compartment,  formed  by  the  two  outer  ver 
tical  partitions  and  the  shell  of  the  tank,  the 
upper  baffle  plate  and  the  screen,  was  placed 
excelsior,  which  rested  on  the  baffle  plate. 
The  superficial  area  of  the  excelsior  was  7.85 
square  feet.  It  was  removed  on  May  IT. 

When  the  water,  in  its  upward  flow 
through  the  tank,  reached  the  last  baffle  plate, 
it  passed  through  the  normal  opening  and  t'he 
space  above  it,  bounded  by  the  shell  of  the 
tank  and  one  of  the  outer  partitions;  and 
thence  it  flowed  over  this  partition  into  the 
central  compartment.  As  described  above, 
this  compartment  was  divided  into  halves  by 
a  central  partition,  which  extended  to  the  ex 
celsior  compartment  at  the  bottom.  From 
one  side  to  the  other,  the  water  passed  by 


flowing  through  the  excelsior  and  underneath 
the  central  partition.  Thence  rising  in  the 
other  half  of  the  central  compartment,  the 
water  overflowed  the  outer  partition,  into  a 
compartment  between  this  partition  and  the 
shell  of  the  tank.  The  outlet  pipe,  6  inches 
in  diameter,  connected  with  the  tank  by  a 
flange  joint  at  the  center  of  this  compartment, 
and  24  inches  below  the  top  of  the  tank. 
From  the  tank,  the  outlet  extended  directly 
into  the  open  compartment  above  the  sand 
of  the  Jewell  filter,  ending  in  an  elbow  and  a 
6-inch  nipple  turned  down.  No  arrangement 
was  provided  to  break  the  stream  of  water  as 
it  entered  the  filter.  The  lower  end  of  the 
nipple  forming  the  outlet  was  on  a  level  with 
the  staves  of  the  outer  tank,  and  35  inches 
above  the  sand.  It  was  12  inches  from  the 
edge  of  the  outer  tank  to  the  center  of  the 
nipple.  At  the  contract  rate  of  flow,  250,000 
gallons  per  24  hours,  the  vertical  velocity  in 
the  iron  tank  was  3.28  lineal  feet  per  minute, 
or  1.2  per  cent,  of  the  velocity  in  a  4-inch 
pipe.  This  tank  was  used  from  May  10  to 
May  19,  inclusive.  On  May  n,  the  excelsior 
was  removed  from  the  inner  compartment; 
but  no  further  changes  were  made.  The  sys 
tem  was  not  in  operation  from  May  19  to  28. 

CLAY  EXTRACTOR. 

This  device  consisted  of  a  rectangular  iron 
tank,  6  by  3  feet,  and  16  feet  high.  It  was 
made  of  o.ig-inch  plates  of  boiler  iron,  riveted 
together,  and  was  divided  into  two  equal  com 
partments  by  a  central  partition.  At  points 
1.75  and  i.o  feet  from  the  top  and  bottom, 
respectively,  there  were  angle  irons  riveted  to 
the  wall  of  the  tank,  and  upon  which  rested 
screens  of  about  o/>25-inch  mesh.  The  space 
between  the  screens  in  each  compartment, 
14.3  feet  in  height,  was  filled  with  crushed 
coke.  The  diameter  of  the  pieces  of  coke 
ranged  from  0.5  to  2  inches,  and  averaged 
more  than  i.o  inch.  A  stay  bolt,  0.5  inch  in 
diameter,  was  passed  through  the  tank  from 
end  to  end,  and  through  the  central  partition 
about  5  feet  from  the  top.  Midway  in  each 
of  the  compartments  at  the  bottom  of  the  ' 
tank,  an  iron  plate,  i  foot  high  and  3  feet 
long,  was  placed  beneath  the  above-men 
tioned  screens,  parallel  to  the  central  parti 
tion.  These  plates  relieved  the  angle  irons 


320 


WATER  PURIFICATION   AT  LOUISVILLE. 


of  some  of  the  weight  of  the  layer  of  coke 
above  them.  In  the  corners  of  each  of  the 
two  compartments  at  the  bottom  of  the  tank, 
where  the  river  water  entered  and  the  wash- 
water  left  it,  curved  iron  plates  were  arranged, 
to  guard  against  accumulations  of  mud  and 
other  deposits.  At  the  center  of  each  side  of 
the  two  lower  compartments,  there  were 
openings,  to  which  4-inch  flanges  were  at 
tached.  The  two  4-inch  pipes  entering  the 
tank  at  ;he  front  by  means  of  these  flanges 
were  used  to  admit  the  river  water  to  the 
tank;  an  1  the  two  corresponding  pipes  at  the 
rear  conducted  the  wash-water  to  the  sewer. 
At  the  center,  on  the  front  side  of  each  of  the 
two  open  compartments  above  the  coke  at  the 
top  of  the  tank,  there  were  openings,  to 
which  the  two  6-inch  outlet  pipes  were  con 
nected  by  flange  joints.  The  two  inlet  river- 
water  pipes,  the  outlet  river-water  pipes,  and 
the  two  wash-water  outlet  pipes,  were  in  each 
case  branches  of  a  single  main  pipe  of  the 
same  diameter;  and  on  the  first  and  last  pair 
of  pipes  gate  valves  were  provided,  with  the 
view  to  using  the  two  compartments  either 
separately  or  together.  In  practice,  however, 
both  compartments  were  used  together,  as 
the  central  partition  was  unable  to  prevent 
the  water  from  passing  from  one  to  the  other. 

It  was  arranged  that,  when  the  coke  should 
become  clogged  and  require  cleaning,  the 
water  could  be  drained  out  through  the  outlet 
leading  to  the  sewer;  and  connections  were 
provided  so  that  the  effluent  of  the  Jewell  fil 
ter  could  be  pumped  through  a  2-inch  pipe 
to  the  open  compartment  at  the  top  of  the 
tank,  and  then  flow  by  gravity  to  the  wash- 
water  outlet  pipe  at  the  bottom.  A  10-  by  18- 
inch  hand-hole,  with  its  center  1.5  feet  from 
the  bottom  and  the  side  of  the  tank,  was 
placed  at  each  end  of  the  tank,  with  the  view 
to  taking  out  some  of  the  clogged  coke  at 
the  bottom,  if  it  should  become  too  much 
clogged  to  be  cleaned  by  the  above-stated 
method  of  washing. 

The  main  inlet  and  outlet  pipes  were  the 
same  as  were  used  with  the  iron  tank  con 
taining  baffle  plates.  On  the  inlet  there  was 
a  meter  and  a  pressure  gauge,  to  show  the 
head  required  to  force  the  water  up  through 
the  clay  extractor.  This  new  device  was  com 
pleted  May  28. 


POLARITE  FILTER. 

The  polarite  filter  consisted  originally  of 
a  layer  of  polarite  placed  between  layers  of 
sand,  with  all  the  filtering  material  resting 
upon  the  underdrains  in  a  large  open  wooden 
tank.  This  tank  was  rectangular  in  form,  23 
feet  long,  10.2  feet  wide  and  7.3  feet  deep,  as 
shown  by  inside  measurements.  It  was  made 
of  2-inch  smooth  pine  planks,  fastened  to  sup 
ports  as  follows:  The  floor  was  supported  by 
eight  pieces  of  timber,  10  by  3  inches,  which 
extended  about  5  feet  beyond  each  side  of 
the  tank.  These  timbers  were  connected  to 
gether  at  each  end  by  planks.  On  each  side 
of  the  tank  there  were  eight  upright  pieces  of 
timber  of  the  same  size  as  those  at  the  bottom, 
and  in  each  case  a  timber  6  by  3  inches  ex 
tended  from  the  end  of  the  bottom  supports 
to  about  midway  on  the  upright  supports. 
The  floor  and  sides  were  laid  first,  and  spiked 
to  the  supports  mentioned  above.  The  planks 
at  the  end  were  fitted  into  a  shallow  vertical 
groove,  which  was  cut  on  the  inside  of  the 
side  planks,  and  the  side  planks  were  spiked  to 
those  on  the  end.  Midway  on  each  end,  there 
was  an  upright  oak  timber,  6  by  6  inches,  to 
which  the  planks  were  also  spiked.  Two  stay- 
rods,  0.75  inch  in  diameter,  passed  length 
wise  through  the  tank,  and  were  fastened  at 
the  ends  to  these  oak  timbers. 

On  the  bottom  of  the  tank,  there  were 
placed  at  right  angles  to  each  other,  two 
layers  of  3-inch  tiles,  with  the  long  dimension 
horizontal,  and  the  ends  about  0.5  inch  apart 
at  the  joints.  The  space  between  the  tiles 
was  filled  with  coarse  gravel.  In  addition  to 
the  tiles  at  the  bottom  of  the  filter,  there  were 
laid  on  one  side,  both  ends  and  across  the 
center  from  end  to  end,  rectangular  troughs 
of  wire,  with  o. 5-inch  meshes.  These  troughs 
were  4  inches  square  in  section,  open  at  the 
bottom,  and  were  intended  to  serve  as  an  aid 
to  the  tiles,  in  conducting  the  filtered  water 
to  the  end  of  the  tank,  where  the  outlet  pipe 
was  placed.  The  slope  of  the  bottom  of  the 
tank  toward  the  outlet,  was  about  i  inch  in 
its  length  of  23  feet.  At  each  of  the  four  cor 
ners,  on  the  inside  of  the  tank,  there  was  con 
structed  a  stand  pipe,  made  of  3-inch  hard 
tile,  with  cemented  joints.  These  pipes  ex 
tended  above  the  level  of  the  water  which 


THE  MACDOUGALL   POLAR! TE  SYSTEM   OF  PURIFICATION. 


.1  •' 


stood  upon  the  sand  when  the  filter  was  in 
operation,  and  were  designed  to  act  as  air 
vents. 

On  the  top  of  the  tile  drains  (and  the  wire 
troughs)  the  following  layers  of  filtering 
material  were  placed,  successively:  6  inches 
of  coarse  gravel;  3  inches  of  coarse  sand:  6 
inches  of  fine  sand;  20  inches  of  polarite;  and 
6  inches  of  fine  sand.  The  original  depth  of 
filtering  material  in  the  polarite  filter,  not 
counting  the  coarse  sand  and  gravel  at  the 
bottom,  was  32  inches,  and  the  area  of  filter 
ing  surface  was  234.8  square  feet,  a  little  more 
than  double  that  of  the  Jewell  filter  (115.8 
square  feet).  The  proposed  area  of  the 
polarite  filter  was  determined  by  Mr.  Mac- 
Dougall,  on  the  assumption  that  the  polarite 
filter  could  be  operated  with  satisfactory  re 
sults  at  one-half  of  the  rate  of  filtration  em 
ployed  in  the  case  of  the  Jewell  filter,  or  about 
50  million  gallons  per  acre  per  24  hours.  A 
rectangular  wooden  trough,  6  inches  wide 
and  6.5  inches  deep,  extended  completely 
around  the  inside  of  the  tank,  4.5  feet  from 
the  bottom.  The  6-inch  inlet  pipe  discharged 
the  effluent  of  the  Jewell  filter  into  this  trough 
at  the  northwest  corner  of  the  tank.  At  the 
southwest  corner  of  the  tank,  a  6-inch  pipe 
led  the  wash-water  from  this  trough  to  the 
sewer.  The  main  outlet  pipe  was  6  inches  in 
diameter,  placed  as  near  as  practicable  to  the 
bottom  of  the  tank,  on  the  end  near  the 
northeast  corner.  The  effluent  of  the  polarite 
filter  discharged  into  the  wrought-iron  reser 
voir,  in  order  to  store  enough  water  for  wash- 
water  during  operation.  Arrangements  were 
made  whereby  this  effluent  could  be  pumped 
under  pressure  through  a  3-inch  pipe  which 
entered  the  polarite  filter  at  the  bottom,  about 
midway  on  the  north  side.  Valves,  meters, 
and  gauges  were  inserted  wherever  conven 
ience  required. 

The  sand  in  the  polarite  filter  was  taken 
from  several  sources.  A  part  of  it  came  from 
lots  which  remained  at  the  pumping  station 
from  the  preceding  year,  and  a  part  was 
taken  from  the  bed  of  the  Ohio  River.  All 
of  these  materials  were  washed  carefully  in  a 
wheelbarrow  with  filtered  water  from  a  hose. 
Analyses  of  the  more  important  filtering  ma 
terials  are  given  beyond. 


Changes  in  the  Polarite  filter. 

A  number  of  changes  were  made  in  the 
polarite  filter  as  follows: 

1.  On  May  11,  it  was  found  that  the  joints 
of  the  air-vents  (stand  pipes  at  the  corners) 
leaked,   and   allowed   some   of  the    water   to 
reach  the  bottom  of  the  filter  without  passing 
through    the    filtering    materials.      The    two 
upper  sections  of  each   vent   were  removed, 
and  the  lower  sections  were  filled  with  filter 
ing  materials,  to  correspond  with   the  main 
filter  layers. 

At  the  same  time  there  were  added  above 
the  filtering  materials  just  mentioned,  5  inches 
of  coarse  coke  and  5  inches  of  fine  coke. 
This  increased  the  depth  of  the  filtering 
materials  to  42  inches,  and  owing  to  the 
fact  that  the  coke  reached  the  sides  of  the 
distributing  trough,  which  was  placed  around 
the  tank  on  the  inside,  the  surface  area  was 
reduced  to  about  200  square  feet. 

2.  On   May  14,  there  were  placed  on  the 
top  of  the  above-mentioned   coke,   2   inches 
of  fine  sand.     This  increased  the  depth  to  44 
inches,  but  the  surface  area  was  unchanged. 

3.  On  May   17,  air  vents  were  placed  in 
the  northwest  and  southeast  corners  of  the 
filter,  as  follows:    Three  pieces  of  pipe,   1.5 
inches  in  diameter,  were  put  through  the  side 
of  the  tank  at  12,  40,  and  48  inches  from  the 
bottom,  respectively;  and  by  the  aid  of  an  el 
bow,  each  pipe  was  extended  above  the  water 
level.    The  object  of  this  was  to  take  out  ac 
cumulations  of  air  at  different  levels  within 
the  filter. 

4.  During  the  period  from  May  19  to  28, 
inclusive,  this  system  was  out  of  service,  and 
a  number  of  changes  were  made.    The  princi 
pal  one  was  the  substitution  of  the  clay  ex 
tractor,  for  the  small  upright  settling  tank,  as 
already  described.     The  upper  layer  of  sand 
and  both  layers  of  coke  were  removed.    After 
the  removal  of  these  materials,  the  lower  lay 
ers  were  washed  by  pumping  filtered  water 
into  the  bottom  of  the  filter  for  about  3  hours. 
During  this  time  about  3,600  cubic  feet  of 
wash-water  were  used.     The  surface  of  the 
6-inch  layer  of  fine  sand,  resting  upon   the 
polarite,  was  leveled,  and  upon  it  were  placed 
3  inches  in  depth  of  fine  coke,  which  had  been 


322 


WATER   PURIFICATION  AT  LOUISVILLE. 


carefully  washed  with  filtered  water  from  a 
hose.  Above  this  coke  layer,  3  inches  of  fine 
sand,  washed  in  the  same  manner  as  the  coke, 
were  placed.  This  left  the  surface  of  the  filter 
below  the  bottom  of  the  distributing  trough, 
and  consequently  the  area  was  restored  to 
234.8  square  feet.  The  depth  of  the  filtering 
material  was  38  inches. 


The  leading  features  concerning  the  sev 
eral  filtering  materials  are  as  follows: 

Polaritc. — Polarite  is  the  trade  name  of  a 
hard,  black,  porous  and  magnetic  iron  sub 
stance,  which  does  not  rust  or  dissolve  in 
water.  It  is  understood  that  it  is  prepared 
from  a  suitable  natural  ore  by  a  patented  pro 
cess,  and  by  crushing  and  screening,  any  de 
sired  size  of  grain  may  be  obtained.  By  vir 
tue  of  its  numerous  and  minute  pores,  in 
which  atmospheric  oxygen  may  be  occluded, 
polarite  is  claimed  to  possess  a  powerful  ac 
tion  in  the  destruction  of  organic  matter  by 
oxidation.  The  chemical  composition  of  the 
polarite  used  in  these  tests  was  as  follows: 

PERCENTAGE   COMPOSITION    OF    POLARITE. 

Silica  (SiO.j) 22.65 

Magnetic  oxide  of   iron  (Fe3O4)      49. 17 

Alumina  (Al  O  I    I  lvith  a  trace  °f  manganese  '  I2   ,(, 
31    \      and  phosphoric  acid.          f  '  ' 

Lime  (CaO) 0.85 

Baryta  (BaO) 0.02 

Magnesia   (MgO) 7.00 

Undetermined,  chiefly  water  and  carbon 8.15 


It  was  found  that  the  nitrogen  in  the  form 
of  albuminoid  ammonia  in  the  polarite  was 
5.4  parts  per  million. 

The  grains  of  polarite  were  very  coarse  for 
a  filtering  material,  as  shown  by  the  following 
mechanical  analysis: 

MECHANICAL    ANALYSIS    OF    POLARITE. 


Effec 
giv 


12. 
5. 
3- 


:nt.  by  we 

100. 0 

93-4 

50.1 

I5.I 

1.6 

0.4 

1.78 


Sand. — There  were  three  lots  of  sand  used 
in  the  polarite  filter;  one  lot  was  coarse,  and 
the  other  two  were  fine  sand.  The  coarse 


sand  resting  upon  the  coarse  gravel  at  the 
bottom  of  the  filter,  and  the  fine  sand  at  the 
surface,  were  taken  from  the  river  bed;  while 
the  fine  sand  forming  the  layer  just  beneath 
the  porlarite  was  obtained  at  the  pumping  sta 
tion,  where  it  had  been  left  by  some  of  the  fil 
ter  companies  from  the  preceding  year.  All  of 
this  material,  as  already  stated,  was  washed 
with  filtered  water  from  a  hose  in  iron  wheel 
barrows.  The  amount  of  organic  matter  re 
maining  on  the  sand  after  washing  is  indi 
cated  by  the  nitrogen  in  the  form  of  albu 
minoid  ammonia,  as  follows: 


Number 

Nitroeen  as 

of 

Source. 

Location  in  Filter. 

Ammoim 

Sand.       ; 

Harts  per 

Million. 

1  6                Riverbed. 

Laver  above  gravel. 

9.2 

17 

Pumping  station. 

Layer  between  gravel 

and  polarite.                     6.S 

18 

River  bed. 

Layer  at  surface.               17.4 

The  efficient  size  of  these  filtering  materials, 
as  shown  by  mechanical  analyses,  was  as  fol 
lows: 

MECHANICAL    ANALYSES    OF     SAND     USED     IN 
THE   POLARITE    FILTER. 


Finer  than  3.90  millimet 
"         "     2 . 04 
"     0.93 
"     0.46 
"        "     0.316 
"     0.182 

Effective    si/.e    (ten    per    cent,    fi 
than   given   diameter   in    millime 
ters) 


07  8 

89.2 

67  6 

2   8 

O.I 

0.1 

Coke. — The  coke  was  of  the  ordinary  com 
mercial  variety.  The  coarse  coke  was  of  the 
grade  commonly  called  nut  size,  and  it  con 
tained  when  new  40.0  parts  per  million  of 
nitrogen  in  the  form  of  albuminoid  ammonia. 
In  the  case  of  the  fine  coke  when  new  the 
nitrogen  in  this  form  amounted  to  49.8  parts. 
For  this  line  of  work  the  amount  of  lime  and 
iron  contained  in  coke  is  of  some  significance. 
The  amounts  of  these  constituents  in  the  two 
grades  were  as  follows: 


Fine  Coke. 
17.43  per  cent. 

0.95     "       " 
1.83     "       " 


The  size  of  the  finer  grade  is  indicated  by 
the  results  of  the  following  mechanical  an 
alyses: 


THE   MACDOUGALL    POLARITE   SYSTEM    OE  PURIFICATION. 


323 


MECHANICAL    ANALYSES   OF    FINE   COKE    USED 
IN   THE   POLARITE    FILTER. 


100.0 
91.3 
83.2 
67.6 
-44-7 
27.6 
18.7 


Finer  tlian    12.0  millimeters. 
5-89 

3-9° 
2.04 
0.93 
0.46 
0.316 

O.IS2 

0.105  3-3 

Effective  size  (ten  per  cent,  finer  than  given 
diameter  in  millimeters)   0.21 


Operation  of  the  Polarite  System. 

The  operation  of  the  polarite  system  was 
divided  into  two  periods,  namely:  From  May 
10  to  19,  and  from  May  28  to  June  12,  1897, 
inclusive.  During  the  intervening  time  be 
tween  the  two  periods  changes  were  made  in 
the  filter,  and  the  clay  extractor  was  substi 
tuted  for  the  small  iron  settling  tank,  as  has 
been  described. 

The  general  features  of  the  operation  were 
arranged  by  the  Water  Company  to  be  as  fol 
lows: 

The  operation  of  this  system  was  under  the 
direction  of  Mr.  MacDougall,  or  his  represen 
tative.  The  required  rate  of  treatment  was 
250,000  gallons  per  24  hours,  equivalent  to 
23.2  cubic  feet  per  minute;  the  system  was 
under  operation  as  continuously  as  practic 
able  from  6.00  A.M.  on  Monday  until  6.00  P.M. 
on  Saturday,  during  each  week.  It  was  also 
understood  by  the  Water  Company  that  no 
chemical  coagulants  would  be  used  in  connec 
tion  with  this  system. 

A  record  of  the  most  important  points  con 
nected  with  the  operation  of  this  system  is  as 
follows: 

Period  No.  i. 

The  first  period  of  operation  extended  from 
May  10  to  May  19,  when  the  system  was  shut 
down  for  alterations  and  repairs  for  a  con 
siderable  length  of  time.  The  river  water 
was  fairly  uniform  in  character  for  the  first 
four  days,  ranging  from  171  to  260  parts  per 
million  of  suspended  solids.  On  May  14  and 
15  a  slight  rise  caused  the  suspended  matter 
to  increase  to  1,260  parts  per  million.  For 
the  remaining  three  days  the  solids  averaged 
486  parts  per  million. 


The  operation  of  the  system  began  on  May 
10  at  9.10  A.M.  At  3.45  A.M.  on  May  11  the 
system  was  stopped  in  order  to  remedy  leaks 
in  the  air  vents  of  the  polarite  filter,  and  to 
add  to  the  filter  10  inches  of  coke,  as  already 
stated. 

Operations  were  resumed  on  May  12,  at 
9.04  A.M.,  but  the  rate  of  filtration  was  re 
duced  to  12.0  cubic  feet  per  minute,  which  was 
about  one-half  of  the  normal  rate.  This  re 
duced  rate  was  held  until  May  13,  at  9.00  A.M., 
when  it  was  increased  to  18.0  cubic  feet  per 
minute  (about  three-quarters  of  the  normal 
rate),  which  was  held  until  May  14,  at  9.44 
A.M.  Up  to  this  time  the  efiluent  was  never 
clear  in  appearance  as  it  left  the  polarite  filter; 
although  the  water  was  clearer  at  this  point 
than  it  was  when  it  left  the  Jewell  filter. 

The  system  was  stopped  on  May  14,  at 
9.44  A.M.,  and  2  inches  of  fine  sand  were  added 
to  the  surface  of  the  polarite  filter,  after  it 
had  been  washed  for  several  hours  by  pump 
ing  filtered  water  through  from  below,  at  the 
rate  of  12  to  14  cubic  feet  per  minute.  Dur 
ing  this  time  2,083  cubic  feet  of  wash-water 
were  used. 

On  May  14,  at  7.46  P.M.,  the  operation  of 
the  system  was  resumed;  and  from  that  time 
until  May  15,  at  9.00  A.M.,  a  solution  of  sul 
phate  of  alumina  was  applied  to  the  water  as 
it  left  the  Jewell  filter  on  its  way  to  the  polar 
ite  filter.  During  this  period  the  rate  of  ap 
plication  of  sulphate  varied.  It  ranged  from 
1 1.09  to  i.oo  grains  per  gallon,  and  averaged 
4.39  grains.  The  rate  of  filtration  was  13 
cubic  feet  per  minute  from  t'he  last  resump 
tion  of  operation  until  May  15,  at  6.00  P.M., 
when  the  system  was  stopped  from  Saturday 
night  until  Monday  morning.  During  the 
greater  portion  of  the  night  of  May  14,  when 
sulphate  of  alumina  was  applied  to  the  water 
as  it  entered  the  polarite  filter,  the  effluent  of 
this  filter  was  clear.  At  all  other  times  it 
possessed  a  decided  turbidity. 

Whenever  the  system  was  out  of  service  it 
was  repeatedly  noted  that  many  air  bubbles, 
some  of  which  were  quite  large,  appeared  on 
the  surface  of  the  water  on  the  polarite  filter, 
near  the  edge  of  the  tank.  On  the  morning 
of  May  17,  the  water  in  this  filter  was  allowed 
to  drain  out,  and  it  was  found  that  there  was 
a  scum  of  aluminum  hydrate,  clay,  etc.,  about 


324 


WATER   PURIFICATION  AT  LOUISVILLE. 


0.25  inch  thick  deposited  upon  the  surface  of 
the  filter.  There  was  also  seen  a  large  num 
ber  of  holes  around  the  edges  of  the  filter, 
some  of  which  ranged  from  3  to  8  inches  in 
width  and  depth.  Air  vents,  as  previously  de 
scribed,  were  inserted  at  this  time,  and  about 
three  wheelbarrows  of  fine  sand  were  added, 
to  fill  the  holes  at  the  sides.  The  thick  scum 
cracked  in  places,  and  the  entire  surface  of  the 
polarite  filter  was  raked.  Filtered  water  was 
pumped  into  this  filter  from  below,  until  the 
gauge  showed  that  the  water  level  was  32 
inches  above  the  bottom.  The  Jewell  filter 
was  put  in  operation  at  13  cubic  feet  per  min 
ute  on  May  17,  11.39  A.M.;  and,  above  the 
point  just  stated,  the  polarite  filter  was  filled 
from  the  top.  This  caused  a  good  many  bub 
bles  to  appear  at  the  surface,  especially  along 
the  edge  of  the  filter.  From  the  beginning  of 
the  operation  of  the  system  on  this  date,  until 
2.28  P.M.,  sulphate  of  alumina  was  applied  to 
the  water  as  it  left  the  Jewell  filter  at  an  aver 
age  rate  of  1.06  grains  per  gallon.  At  2.00 
P.M.  the  rate  of  filtration  was  increased  to  18 
cubic  feet  per  minute;  at  4.00  P.M.  it  was  in 
creased  to  23.5  cubic  feet;  and  at  4.45  P.M. 
it  was  decreased  to  18  cubic  feet.  The  system 
was  out  of  operation  from  5.00  to  5.21  P.M. 
on  this  date,  in  order  to  allow  air  to  escape 
from  the  polarite  filter.  The  surface  of  this 
filter  was  also  raked,  and  the  water  above  the 
sand  drained  off  to  a  depth  of  i  foot  at  this 
time.  From  May  17,  at  5.21  P.M.,  until  May 
19,  at  8.45  A.M.  (the  close  of  the  first  period 
of  operation)  this  system  was  operated  at  a 
rate  of  about  18  cubic  feet  per  minute,  with 
out  any  special  features  of  importance.  The 
effluent  of  the  polarite  filter  was  at  no  time, 
during  this  portion  of  the  period,  free  from  a 
decided  turbidity. 

Independent  of  repairs,  and  of  the  wash- 
water  pump,  this  system  required  the  atten 
tion  of  one  regular  attendant  to  control  the 
rate  at  which  the  river  water  entered  the  set 
tling  tank;  to  regulate  the  outlet  valves  of 
the  Jewell  and  polarite  filters,  so  that  the 
depth  of  water  upon  them  was  approximately 
constant;  to  apply  sulphate  of  alumina  solu 
tions;  and  to  agitate  and  wash  the  Jewell  filter. 
During  this  period,  from  May  10  to  19, 
there  were  available  by  arrangement,  7.48 
days,  of  24  hours,  in  which  to  operate  the  sys 
tem.  Of  this  time  5.73  days  were  devoted 


to  regular  operations,  and  the  balance  of 
1.75  days  (23  per  cent,  of  the  period)  to  re 
pairs  and  changes.  Of  the  5.73  days  de 
voted  to  regular  operations,  3.8  per  cent,  of 
the  time  was  occupied  in  washing  and  agita 
ting  the  Jewell  filter. 

The  quantity  of  water  passed  through  the 
Jewell  filter  during  this  period  was  120,865 
cubic  feet,  and  the  quantity  of  effluent  of  the 
polarite  filter  was  practically  the  same.  This 
made  the  actual  rates  of  treatment  of  water 
by  the  two  filters,  expressed  in  different 
forms,  as  follows: 

AVERAGE   ACTUAL   RATES   OF    FILTRATION 
IN    THE    POLARITE   SYSTEM. 

Jewell       Pobrite 
Filter.        Filter. 

Gallons  per  24  hours 164  ooo      164  ooo 

Cubic  feet  per  minute 15-2  15.2 

Million  gallons  per  acre  per  24  hours        62       *3o.5-f36.o 
*  Original  area,     f  Modified  area. 

Of  the  total  quantity  of  water  treated, 
120,865  cubic  feet,  sulphate  of  alumina  was 
applied  to  11,919  cubic  feet  (9.9  per  cent,  of 
total  quantity)  at  an  average  rate  of  3.80 
grains  per  gallon.  This  amount  of  sulphate 
of  alumina  was  equivalent  to  0.37  grain  per 
gallon  of  the  total  quantity  of  water  treated 
during  the  period. 

The  accumulation  of  sediment,  etc.,  on  the 
surface  of  the  Jewell  filter  was  removed  in  a 
manner  somewhat  different  than  was  pre 
viously  the  case,  in  that  the  filter  was  washed 
less  frequently,  and  surface  agitation  was  em 
ployed  more  frequently,  with  the  modification 
that,  at  the  close  of  agitation,  the  water  above 
the  top  of  the  staves  of  the  inside  tank  was  al 
lowed  to  pass  to  the  sewer.  The  average 
quantity  of  unfiltered  water  thus  wasted  at  the 
time  of  each  agitation  was  about  200  cubic  feet. 

A  record  of  the  washes  of  the  filter  is  as  fol 
lows: 

WASHING   OF    THE    JEWELL     FILTER— PERIOD 
No.  1. 


"o  " 

Date  of  Washing. 

tt 

|l  i»[| 

.g! 

II 

Day. 

Hour 

*O    U5 

5  £  2 

|||l 

i^ 

z 

a, 

a 

£ 

?, 

I* 

May  10 

5.2O  P.M. 

2om. 

750 

i°953 

0 

2 

"     ii 

4.30       " 

2om. 

739 

11815 

0 

3 

"     '4 

10.47  A.M. 

lorn. 

529 

40720 

6 

4 

"     18 

4.25   P.M. 

iSm. 

644 

41  938     14 

5t 

'      19 

15439 

4 

Washed  by  Water  Company  to  prevent  stopping  at 
night,  in  the  absence  of  instructions  to  the  operator  from 
Mr.  MacDougall. 

f  Washed  by  Water  Company,  preparatory  to  use  with 
Water  Company's  devices. 


THE  MACDOUGALL   POLARITR   SYSTEM  OF  PURIFICATION. 


325 


As  the  operation  of  this  system  progressed,   ••  greater,   as   the   agitations   wtihout    washing 

f    TiMvpll    filtpr   \vn«    \\-nsliprl    Ipse    frpnufiitlv          iiirrenspd 


the  Jewell  filter  was  washed  less  frequently, 
and  agitated  more  often,  as  seen  by  the  next 
table,  in  which  the  principal  data  are  recorded. 
It  will  be  noted  that  the  loss  of  head 
following  an  agitation  gradually  became 


increased. 

The  polarite  filter  did  not  become  clogged 
except  by  the  air  which  was  trapped  in  its 
pores  at  times.  The  bulk  of  this  air  rose  to 
the  surface  when  the  outlet  was  closed. 


AGITATIONS    OF   THE    JEWELL    FILTER— PERIOD    No.  1. 


Date  of 

Agitation. 

Period  of 

Quantity  of  Filtered 

Water.  Cubic  Feet. 

Initial  Loss  of  Head 
in  Feet  following 

Agitation. 

Day. 

Hour. 

Agitation. 
Minutes. 

Since  Last 
Washing. 

Since  Last. 
Agitation. 

Agitations  -Rate 
23.5  Cubic  Feet 
per  Minute. 

1897 

2 
3 

'3 
13 

9.05       " 

1.14  r.M. 

2f>m. 
23m. 

16674 
20665 
24  869 

4755 
3991 

4.0 
3-9 

5 
6 

13 
'4 

10.09     " 

4.07  A.M. 

24m. 
23111. 

39J25 
45095 

4256 
5970 

5-2 

6.0 

8 

15 

4.49  A  M. 

26m. 

6864 

3  Sio 

3-i 

•J  ao    P  M 

' 

' 

16  157 

C               >   M 

'3 
'4 
15 
1  6 

17 

17 
18 
18 

S.I9           ' 
11.40           ' 

2.45  A.M. 

2  1  m  . 

22111. 

23899 
27038 
30015 

2  770     . 
3  137 
2979 

5-7 
6-5 

6.7 

17 
18 

18 

18 

8.00       ' 

23m. 

34  793 
36  ->i6 

1484 

7-0 

18 

I  728 

20 

18 
18 

2.00  P.M. 

2om. 

39  9  '4 

970 

7-i 

2    6 

22 
23 

18 
19 

11.39       ' 

3-34  A.M. 

22m. 

23m. 

6  926 
10691 

3  299 

3  705 

2.6 

2-7 

Period  No.  2. 

This  period,  following  repairs  and  changes 
which  have  been  enumerated,  extended  from 
May  28,  12.35  P.M.,  until  June  12,  6.00  P.M., 
the  close  of  the  tests  of  this  system. 

During  this  time  the  system  was  operated 
continuously,  excepting  from  Saturday  nights 
until  the  following  Monday  mornings,  at  ap 
proximately  the  full  rate.  The  exact  rate 
called  for  in  the  contract  was  23.2  cubic  feet 
per  minute;  but  it  was  the  general  custom 
throughout  all  these  tests  to  maintain  the  rate 
as  nearly  to  23.5  cubic  feet  as  practicable. 
There  were  no  delays,  changes  or  repairs  of 
importance  during  this  period. 

The  river  water  contained  very  little  mud 
at  the  beginning  of  this  period,  but  mostly 
very  fine  clay  particles,  averaging  in  amount 
about  90  parts  per  million  of  suspended  mat 
ter  for  the  first  two  days:  and  the  effluent  of 
the  polarite  filter  was  decidedly  turbid. 


On  May  31  and  June  i,  sulphate  of  alu 
mina  was  applied  to  the  water  as  it  flowed  to 
the  Jewell  filter,  as  follows:  May  31,  7.51  to 
8.45  A.M.,  0.60  grain  per  gallon;  May  31, 
9.00  A.M.  to  3.00  P.M.,  0.24  grain;  May  31, 
5.00  to  9.00  P.M.,  0.21  grain;  May  31,  11.30 
P.M.,  to  June  i,  3.05  P.M.,  0.18  grain  per  gal 
lon.  During  those  portions  of  the  time  be 
tween  May  31,  7.51  A.M.,  and  June  1,3.05  P.M., 
which  are  included  above,  there  was  no 
application  of  chemicals.  From  June  i 
3.05  P.M.  to  5.20  P.M.,  sulphate  of  alumina  at 
the  rate  of  o.  18  grain  per  gallon  was  applied 
to  the  water  as  it  left  the  Jewell  filter  on  its 
way  to  the  polarite  filter.  After  this  there  was 
no  further  application  of  chemicals. 

In  the  absence  of  rains  in  the  Ohio  Valley, 
the  river  water  rapidly  became  clearer,  and 
during  the  remaining  portion  of  this  test  the 
suspended  solids  averaged  only  about  30  parts 
per  million.  The  effect  of  this  is  shown  very 


326 


WATER   PURIFICATION  AT  LOUISVILLE. 


clearly  by  the  fact  that  from  May  31  till  June  8 
the  Jewell  filter  was  neither  washed  nor  agi 
tated  during'  continuous  operation  at  the  nor 
mal  rate.  During  this  time,  without  any  ad 
ditional  application  of  chemicals  (a  iarg;e  por 
tion  of  the  above-stated  applications  remain 
ing  in  and  upon  the  filters),  the  effluent  was 
clear  or  slightly  turbid.  At  no  time,  however, 
was  it  bright  and  perfectly  free  from  visible 
suspended  matter. 

In  addition  to  the  washing  at  the  beginning 
of  this  period  the  Jewell  filter  was  washed  on 
May  31,  7.19  A.M.,  and  on  June  n,  8.53  A.M., 
the  quantities  of  effluent  of  the  polarite 
filter  used  for  wash-water  being  543  and  644 
cubic  feet,  respectively.  The  quantity  of 
water  filtered  "between  the  last  two  washings 
was  315,199  cubic  feet.  The  Jewell  filter  was 
agitated,  and  about  200  cubic  feet  of  unlii- 
tered  water  drained  from  the  surface  of  the 
sand,  eight  times  during  the  last  three  days 
of  the  eleven  days  between  washings,  as  fol 
lows: 

AGITATION  OF  JEWELL  FILTER— PERIOD  No.  2. 


Quantity  of  Filtered  Water. 

Date  of  Agitation. 

Cubic  Feet. 

of  Agi- 

Period  of 
Agitation. 

Date. 

Since  Last 

Since  Last 

,897. 

Washing. 

Agitation. 

1 

"26      :              9 

2.00      " 

31  m 

260611 

33751 

27      |             10 

6.35A.M. 

3om 

282  914 

22  303 

28 

IO 

4.  51  P.M. 

3  nil 

296558 

12644 

29 

10 

9-30      " 

2401 

302  358 

5  Soi 

30               10 

12.  OO     " 

24111 

395  204 

2845 

3i 

II     3.OOA.M. 

25111 

308  735 

3  531 

32 

II 

7.17      " 

34  m 

313  844 

5  109 

The  data  on  loss  of  head  before  and  after 
each  agitation  are  not  complete,  but  it  may 
be  stated  that  the  latter  agitations  did  very 
little  in  decreasing  the  frictional  resistance  of 
the  sand  layer,  and  that  the  filter  was  exceed 
ingly  dirty  on  June  1 1,  when  it  was  absolutely 
necessary  to  wash  the  filter. 

During  this  period  the  polarite  filter  was 
not  washed,  raked,  or  scraped,  and  at  the 
close  of  June  12,  the  loss  of  head  was  21 
inches,  with  the  normal  rate  of  filtration. 

It  was  also  found  that  the  clay  extractor 
did  not  become  clogged  during  service.  Boih 
compartments  were  regularly  used,  although 
neither  of  them  was  washed.  The  acting  head 
necessary  to  force  the  water  through  this  de 
vice  remained  1.9  feet  during  this  period. 


From  May  28  to  June  12,  there  were  avail 
able  by  arrangement  12.22  days  of  24  hours, 
in  which  to  operate  this  system.  Of  this  time, 
1 2.07  days  were  devoted  to  regular  opera 
tions,  and  the  balance  of  0.15  day  was  de 
voted  to  unavoidable  delays,  largely  in  mak 
ing  preparations  to  apply  sulphate  of  alu 
mina.  Of  the  12.07  days  devoted  to  regular 
operations,  1.6  per  cent,  of  the  time  was  oc 
cupied  in  washing  and  agitating  the  Jewell 
filter. 

The  quantity  of  water  passed  through  the 
Jewell  filter  during  this  period  was  397,355 
cubic  feet; 'and  the  quantity  of  effluent  of  the 
polarite  filter  was  substantially  the  same. 
About  399,000  cubic  feet  of  water  passed 
through  the  clay  extractor,  the  increase  here 
(1645  cubic  feet,  equal  to  0.4  per  cent,  of 
total)  being  due  to  the  water  which  was 
drained  from  the  surface  of  the  Jewell  filter. 
This  made  the  actual  rates  of  treatment  of 
water  by  the  three  devices,  expressed  in  dif 
ferent  forms,  as  follows: 

AVERAGE    ACTUAL    RATES  OF  FILTRATION   IN 
THE  POLARITE  SYSTEM. 


Gallons  per  24  hours. .. 

Cubic  feet  per  minute. . 

Million  gallons  per  acre 

per  24  hours 


246  ooo 
22.9 


245  ooo 
22.  S 


245  ooo 

22.8 


Of  the  total  quantity  of  water  treated, 
397,355  cubic  feet,  sulphate  of  alumina  was 
applied  to  40,328  cubic  feet  (10  per  cent,  of 
total  quantity)  at  an  average  rate  of  0.25  grain 
per  gallon.  This  amount  of  sulphate  of  alu 
mina  was  equivalent  to  0.026  grain  per  gallon 
of  the  total  quantity  of  water  treated  during 
this  period. 

QUALITY  OF  THE  OHIO  RIVER  WATER  AFTER 
TREATMENT  BY  THE  POLARITE  SYSTEM. 

In  the  next  two  tables  are  presented  sum 
maries  of  analytical  results,  showing  the  bac 
terial  efficiency  of  the  system,  and  also  the 
percentage  of  removal  of  organic  matter  from 
the  river  water  by  it.  Beyond  these  tables 
are  the  results  of  individual  bacterial  analyses 
of  the  river  water,  and  of  the  water  after  it 
passed  through  the  several  devices  compris- 


THE  MACDOUGALL  POLAR1TE  SYSTEM   OF  PURIFICATION. 


ing  the  system;  and  also  the  results  of  chemi 
cal  analyses  of  the  water  at  different  stages 
of  treatment.  For  further  information  con 
cerning-  the  composition  of  the  river  water 
during  this  period,  in  addition  to  that  shown 
by  the  summaries  of  results,  reference  is  made 
to  Chapter  I. 

The  summaries  of  analytical  results  are  di 
vided  into  two  periods,  which  are  the  same 
as  have  been  used  in  the  foregoing  pages  con 
cerning  the  operation  of  this  system.  It  will 
be  noted  at  once  from  the  summaries  that 
the  river  water  was  quite  muddy  during  the 
first  period:  while  during  the  second  period 
it  was  very  clear,  comparatively  speaking. 
During  the  two  periods,  the  suspended  solids 
in  the  river  water  averaged  004  and  40  parts 
per  million,  respectively. 

As  was  reported  to  you  at  the  time  of  oc 
currence,  the  collection  of  samples  for  anal 
ysis,  during  the  first  day  of  operation  of  this 
system,  was  informally  protested  by  Mr.  Mac- 
Dougall.  on  the  ground  that  this  system  was 
not  yet  ready  for  normal  work.  No  official 
notice  was  received  as  to  the  time  when  this 
protest  was  withdrawn,  if  at  all,  and  no 
further  mention  of  the  subject  was  made  to 
the  writer. 

Owing  to  the  fact  that  so  many  changes 
were  made  during  the  first  period,  in  an  effort 
to  adapt  the  system  to  the  purification  of  the 
Ohio  River  water,  it  does  not  seem  fair  to 
give  the  results  obtained  during  this  portion 
of  the  operation  serious  consideration. 

Concerning  the  results  obtained  during  the 
second  period,  following  several  changes,  it 
will  be  seen  that  the  system  accomplished  no 
substantial  bacterial  purification  of  the  water 
until  sulphate  of  alumina  was  applied  to  the 
water,  as  it  flowed  to  the  Jewell  filter.  It 
further  appears  that  the  aluminum  hydrate, 
deposited  upon  and  within  the  Jewell  filter, 
and  which  was  not  removed  to  a  marked  de 
gree  by  the  surface  agitations  of  the  sand,  or 
by  the  single  short  washing  which  this  filter 
received  after  the  application  of  sulphate  of 
alumina  ceased,  was  clearly  a  more  important 
factor  in  the  purification  of  the  river  water, 
than  was  the  polarite. 

The  coke  in  the  clay  extractor  contained 
lime,  metallic  iron  and  organic  matter.  The 
latter  served  as  a  food  for  the  river  water  bac 


teria;  and  while  there  was  no  increase  after 
the  second  day  of  operation  in  the  albu 
minoid  ammonia  in  the  water  as  it  passed 
through  the  extractor,  the  growths  of  bacteria 
continued  until  nearly  the  close  of  operations. 
It  was  especially  noticeable  that  the  growths 
were  greatest  for  a  short  time  following  a 
period  of  rest,  such  as  the  first  few  hours  of 
operation  on  Monday  mornings. 

The  lime  and  metallic  iron  in  the  coke 
were  steadily  removed  by  the  carbonic  acid 
contained  in  the  river  water.  This  explains 
the  usual  increase  of  about  -2  parts  in  the  alka 
linity  of  the  water  during  passage  through  the 
clay  extractor.  The  still  greater  increase  in 
alkalinity  of  the  water,  during  passage 
through  the  polarite  filter,  is  similarly  ex 
plained  by  the  coke  layers  in  this  filter. 

It  was  found,  from  an  average  of  three  sets 
of  analyses  on  June  4,  that  the  river  water  was 
practically  saturated  with  atmospheric  oxygen 
at  that  time,  and  that  the  effluent  of  the 
polarite  filter  contained  about  90  per  cent,  of 
that  necessary  for  saturation  at  the  actual 
temperature  (21°  C). 

Contrary  to  experience  sometimes  met 
with  effluents  of 'filters  containing  coke,  the 
oxygen  consumed  results  were  apparently 
not  affected,  practical}'  speaking,  by  the  iron 
and  organic  matter  contained  in  the  coke.  In 
all  cases,  the  nitrogen  in  the  form  of  albu 
minoid  ammonia,  and  the  residue  on  evapora 
tion,  were  determined  in  the  water  as  col 
lected,  and  also  after  it  had  been  passed 
through  a  Pasteur  filter.  The  difference  in 
the  corresponding  results  is  recorded  in  each 
case  as  the  amount  in  suspension.  During 
the  last  few  days  of  the  tests,  the  effluents 
were  so  clear  that  the  amount  of  suspended 
matter  could  not  be  satisfactorily  weighed,  al 
though  it  was  generally  visible  in  minute 
quantities.  With  regard  to  the  nitrogen  in 
the  form  of  albuminoid  ammonia,  which  was 
suspended  in  the  effluents  at  this  time,  the  an 
alyses  indicate  that  small  amounts  were  pres 
ent,  although  they  approached  so  nearly  to 
the  limits  of  accuracy  of  the  method  of  an 
alysis  that  full  weight  cannot  be  given  to 
them. 

In  conclusion,  it  may  be  stated  that  the 
evidence  obtained  during  these  tests,  taken  as 
a  whole,  shows  that  the  MacDougall  Polarite 


WAFER  PURIFICATION  AT  LOUISVILLE. 


System  (which  was  investigated  with  the  view 


to    dispensing   with    the 

use    of    coagulating 

chemicals)  was  not  applicable,  in  the  form  in 

SUMMARY 

OF    THE    AVERAGE 

RESULTS      BY 

DAYS     OF     BACTERIAL 

ANALYSES     OF     THE 

OHIO     RIVER     WATER 

BEFORE     AXI) 

AFTER 

TREATMENT   BY   THE   POLARITE  SYSTEM. 

i 

Jeriod  No.    1  . 

Bacte.iap 

cr  Cubic  C 

,ptim,.K,r 

Bacterial  Efficiency. 

D;  tc. 

1897. 

River 

Polarile 

[ewell 

I'nlarite 

Water. 

Effluent. 

Effluent. 

Kilter. 

Filter. 

May  10 

15  300 

7  500 

14  900 

51.0 

2  .  6 

"     II 

1  1  Soo 

3  600 

9500 

69.5 

19.6 

"       12 

31  ooo 

9  700 

30  ooo 

68.7 

3-2 

"     13 

36  200 

16000 

34  9"" 

55-7 

3-6 

"     M 

52400 

38  200 

72  200 

27.0 

-38.7 

"     '5 

49400 

19  5oo 

22  70O 

60.  5 

54.0 

"     17 

22  6OO 

9  ooo 

21    IOO 

60    2 

7-1 

"     18 

16  500 

13900 

14  900 

15-7 

9-7 

"     I9 

12  100 

17  ooo 

10  300 

-  45-o 

14.9 

which  it  was  tested  by  this  Company,  to  the 
efficient  and  economical  purification  of  the 
Ohio  River  water. 


Period  No.  2. 


Bacter 

,  per  Cu 

bic  Centimeter. 

Bacterial  Efficiency. 

Date. 

u- 

j 

j 

s 

1897. 

^ 

V 

c 

<u  5 

u       !             u 

-S 

II 

15E 

'is 

xS 

"35 

§5 

.~  ^ 

£  £ 

"c  •*" 

£  W 

£  fe 

"o  ^ 

X 

W 

A 

0. 

u 

A 

a, 

May   28      7900 

8  300 

5  360 

3  645   -    5 

32 

54 

29      7  700 

7  600 

5  100 

3  77°          i          34 

51 

"       31 

2  560 

10  300 

3  280 

2  040  —  303   —  28 

20 

June    i 

2  2OO 

2  8lO 

2470 

I  270    —  28        —  12 

42 

2     i  910 

770 

i  157 

716 

7 

37 

63 

3      i  39" 

530 

388 

2^0 

—   10 

72 

82 

4        97" 

490 

194 

i  So 

-  53 

80 

81 

'  '         5        710 

190 

158 

116 

-67 

78 

84 

7        770 

1  60 

222 

192 

-  50 

71 

75 

S:       640 

260 

IlS 

81 

-  97 

82 

87 

9        490 

.    9  1  o 

78 

44 

-  86 

84 

91 

10'       460 

700 

55 

45 

-  52 

88 

90 

"       n        470 

547 

48 

36 

-  16 

90 

92 

12           590 

590 

40 

36 

0 

93 

94 

SUMMARY  OF  THE  RESULTS  OF  CHEMICAL  ANALYSES  OF  THE  OHIO  RIVER  WATER,  BEFORE 
AND  AFTER  TREATMENT  BY  THE  POLARITE  SYSTEM,  SHOWING  THE  REMOVAL  OF  OR 
GANIC  MATTER,  AS  INDICATED  BY  THE  NITROGEN  AS  ALBUMINOID  AMMONIA,  AND  BY 
OXYGEN  CONSUMED. 

(Results  in  Parts  per    Million.) 
Period    No.    1  . 


. 

.      , 

Removal 

Date. 

>gen 

1897. 

Water. 

Effluent. 

Effluent. 

Effluent. 

Effluent. 

Water. 

Effluent. 

Effluent. 

Filter. 

Fiiter. 

May  10  )_ 

.282 

.112 

.108 

60 

62 

4-5 

2.0 

1.8 

56 

60 

"       12 

.348 

.!76 

.140 

51 

60 

5-3 

2-7 

2.4 

49 

55 

"       13 

.406 

.232 

.160 

43 

60 

6.0 

3-5 

1.4 

42 

77 

'       14 

.884 

•334 

.no 

62 

8S 

17.2 

6.8 

2.4 

60 

86 

'       15 

1.042 

•396 

.116 

62 

89 

I6.3 

6.0 

2.0 

63 

88 

"       17) 

;;    is 

•448 

.260 

.130 

42 

71 

10.4 

4.9 

2.9 

53 

62 

"    19) 

Period    No.    2. 


Date. 

u     . 

Uj 

^ 

• 

u 

,897. 

v  v 

3  - 

U  4; 

-  = 

u  S 

=•  = 

•-  5 

V.    V-' 

S  s 

-5  = 

.—  - 

>,- 

"B  £ 

•E  5 

S  3 

«^> 

£E 

f  E 

"HE 

^c 

"c  E 

s> 

*^E 

c  E 

U  Jj 

°£ 

ww 

^W 

H« 

-w 

P-W 

a« 

w 

B-W 

w 

May  28     / 
"      29     i 

.146 

.152 

.108 

.096 

-4 

26 

34 

3-5 

3-2 

2.7 

2.5 

9 

23 

29 

'      31    r_ 
June     i    ) 

.138 

.144 

.092 

.098 

-4 

35 

29 

2.8 

2.6 

2.3 

1.8 

7 

18 

36 

2     | 

3    i 

.166 

.148 

.106 

.102 

n 

36 

39 

3-1 

2.7 

2.3 

I.g 

13 

26 

39 

»    J| 

.180 

.166 

.112 

.096 

8 

38 

47 

3-1 

2.4 

1.9 

1.9 

23 

39 

39 

••        8     f 

.186 

.144 

.126 

.104 

23 

32 

44 

2.4 

2.3 

1.8 

1-4 

4 

25 

42 

"        9    ( 
1      10    ) 

.164 

.132 

.106 

.078 

20 

35 

52 

2.2 

2.0 

1.6 

1-5 

9 

27 

32 

"        12     \ 

.176 

.122 

.094 

.082 

31 

47 

53 

2.2 

2.1 

1.6 

i.3 

5 

27 

41 

THE  MACDOUGALL   POLARITR   SYSTEM   OF  PURIFICATION. 

O   r~  m  Q   "i  O   O  OOOOOOOO-r>OO"im  OOCOTOOOO'"  c^co    t  <r 

-ro  fi  O  o  T  T          c*  o  -fj  q  q  o  i^  m  r^  r-i  M  q  o  -rco  o  -r  w  m  -r  tn  ./>  ct  o  q  q 

r-io'-'-do'd         oor^oo>o«  M-C-T--OOOOOOO 

•Euiuiniv  paAios^iQ  I       o  o  o  o  o  o  o         cTo  6~o"  bo^ooooooo          o~o"^'o  o  o  o  o  o  u  o  c  c 


•papuadsns  |         T • 


-  -t  -t  o  o  •- 


CO     T     OQQQOOO 
oo    J;    ooooooo 


oooobo^o     -.    ooooooooooooo    ^-    oocoooooooooo 


o      o  -  o 


O   O    O   O   O   O      3 


O"NN"OOOOOOO 


o    2    ocTcTooJooooooo 


-  o  «  o  o 


c  > 


C     I      I      I      !      I 

u  M   ~t  r^  0s  •-» 


<  o  o<  o  o 


329 


33° 


WATER  PURIFICATION  AT  LOUISVILLE. 


BACTERIA    PER    CUBIC    CENTIMETER    IN    THE    OHIO    RIVER    WATER1    BEFORE    AND    AFTER 
TREATMENT   BY  THE    POLARITE   SYSTEM. 


Date. 

Hour. 

Rate  of 
Fi  tration. 
Cubic 
Feet  per 
Minute. 

Bacteria  per  Cubic  Centimeter. 

Remarks. 

River 
Water. 

Settling  Pipe 
Effluent. 

Jewell 
Effluent. 

Polarite 
Effluent. 

1897 
May   10 
"       10 

"          10 
"         10 
"          10 

"      10 

10 

"      ii 
"      ii 

"        12 
"         12 
"        12 
"        12 

"        12 
"        12 
"        12 
"        12 

"        13 
13 
13 
13 
13 
13 
13 
13 
13 
13 
'3 
M 
14 
14 
14 
14 
14 
15 
15 
15 
15 
15 
15 
15 
15 
15 
17 
17 
17 
17 
"       IS 
"       18 
"       18 
"       18 
"       18 
"       18 
"       18 
"       18 
"       18 
"       18 
"       19 
19 
IQ 

11.00  A.M. 
I.I5  P.M. 
3-°4      " 
5.00      " 
S.io     " 
9.U5     " 

11.00       " 

23-5 
23.5 
23-5 
23-5 
23.5 
23-5 
23-5 

5  800 
6  400 

5  800 

II  OOO 

10450 

8  300 
4500 
3490 
3  (>9° 

21  IOO 
1  8  200 

15  ioo 

15  800 

13  too 
8  900 

12  22O 

8550 

10  500 

*  Application    of    sulphate    of    alu 
mina  began  at  7.46  P.M. 

f  Application    of    sulphate    of    alu 
mina  stopped  at  9.00  A.M. 

17  ooo 

13  700 

3.00     " 
10.30     " 
11.30     " 

12.30  P.M. 
2.40       " 

4-45     " 
5.00     " 
9.00     " 

II.OO       " 
I.OO  A.M. 

3.00    " 
5.00     " 
8.00     " 
g.oo     " 
10.00     " 

12.  OO  M. 
2.OO   P.M. 

4.00     " 
9.00     " 

1  1  .  OO       " 
I.OO  A.M. 

3.00     " 
5.00     " 
9.00     " 

g.OO    P.M. 
II.OO       " 
I.OO  A.M. 
3.00       " 
5-3"       " 
7.OO       " 
g.OO       " 
II.OO       " 
I.OO  P.M. 
3.OO       " 
5.30       " 
3.30       " 
5.05       ' 
g.OO       " 
II.OO       " 
I.OO  A.M. 
3.30       " 
5.00       " 

9  oo     " 
11.00     " 

I.OO  P.M. 

3.00    " 
5.30   •' 

9.00     " 

II.OO       " 

10.  0 

ii  Soo 
45  7oo 
46  500 
43  ioo 

42  900 

12.  O 
12.0 

12  700 

19050 

34700 
38600 

12.  O 
"•5 
12.0 
12.0 
12.  O 
2.0 
2.0 

7300 

5  250 
4  190 
3  no 
27950 
19  200 
19  500 

36  ooo 
25  ooo 

17500 

12  050 
18  950 
39000 
60000 

21  700 

24  ioo 

33000 
38  7OO 
39700 

35  300 

8.0 

8.0 
8.0 
S.o 
8.0 
8  o 
8.0 
8.0 
8.0 
8.0 
3.0 
3-0 
3.0 
3-0 
3-0 
3-o 
3-0 
3-o 
4.0 
3-o 
3-5 
8.0 

15  900 
7  700 
it  500 

20  80O 
19300 

15  ioo 

20  500 

18  200 
81  500 
64  500 
21  900 
22  6OO 
17400 
19  800 
24000 

37  ooo 
31  700 
13  800 
13  750 
8  500 
9  500 
9400 

48  ooo 
37  200 

21  5OO 

54100 

39  ooo 
18  900 
38500 
45  ioo 
255  ooo 
64  200 
*  1  7  ooo 
13  200 
15  ooo 
15  ooo 
32  400 
19500 
fi3  500 
32  500 
24500 
33750 
18000 
34500 
27  200 
12  5OO 
IO  IOO 
12  5OO 
II  400 

16  900 
1  8  500 
30500 
13900 
9  1  20 
10640 
17  200 
8  900 
9700 
8  400 
12  800 

36  500 
45  200 

1 

36  Soo 



49  ioo 
62  700 
6  1  ooo 

57  ioo 

63900 

59  700           64  500 

24  500 

26400 

8.0 
8.0 
8.0 
8.0 
S.o 
8.0 
8.0 

1  8  800 

8  900 
8  700 
9300 
ii  500 
8  600 
21  gOO 
1  8  900 
14  800 
15  ooo 
27  300 
8  ooo 
3900 
4  800 
27  800 
18  500 

16  ioo 

21  200 

8.0 
8.0 
8.5 
8.0 
8.0 
8  o 

19  500           10  710 

9  200 

3.00    " 

5.00     " 

8.0 
8.0 

12  IOO 

1  As  a  matter  of  convenience,  the   numbers  of   the  bacterial  samples   are  omitted.     Samples   Nos.  5809  to  5962 
were  collected  from  May  10  to  19,  and  samples  Nos.  6150  to  6472  from  May  28  to  June  12. 


THE  MAC  DOUG  ALL   FOLAKITF.    SYSTEM   OF  PURIFICATION. 


33' 


BACTERIA    PER    CUBIC    CENTIMETER    IN    TIIF,    OHIO    RIVER    WATER     BEFORE    AXD    AFTER 
TREATMENT    BY    THE    POLARITE    SYSTEM.— Continued. 


Rate  of 

Filtration. 

B 

icteria  per  Cu 

bic  Centimes 

Dale. 

Hour. 

Cubic 
Feet  per 
Minute. 

River 
Water. 

Clay 

Extractor 
F.fflui:nt. 

Jewell 
Effluent. 

Polarite 
Effluent. 

Remarks. 

1897 

"       28 

6  450 

4400 

"       28 
"        29 

'        29 

g.oo 

1.  00  A.M. 

3  oo     " 

23.5 
23-5 
23-5 

8  500 

IO  IOO 

6  loo 

8  300 
5  600 
9  200 

3  660 
3  750 
3900 
4  900 

2  890 

3  MO 
3  1  20 
3  120 

'        29 
29 
29 

1       3 
1       3 
1       3 
1       3 
1       3 
une 

g.oo     " 

12.00  M. 
5.OO  I'.M. 
g.OO  A.M. 
11.00       " 
5.OO  P.M. 
8.00       " 
11.00       " 

23.5 
23-5 
23.0 
23-5 
23-5 
23-5 
23-5 
23.5 

6  700 
8000 

2  890 
2  420 
2010 

2  930 

7400 

7  100 
8  400 

21  OOO 
21  500 

2970 

3  200 

4  ioo 

5400 
6  500 
6950 
*5  120 
3  19° 
2  400 
2  ggO 
2  720 

3  220 

4950 

5  too 

3750 

2  150 

I  440 
1  580 
I  270 

*  Application    of    sulphate   of    alu 
mina  began  at  7.51  A.M. 

5.00     " 

23-5 

3  Coo 

3710 

242O 

1  350 

i  935 

" 

II.  OO       " 
4.0O  P.M. 

23.5 
23.5 

I  580 
i  850 

I  650 

2  520 

2  720 
fl950 

i  750 
t    640 

i  695 

f  Began  application  of  sulphate  o: 

" 

11.00       " 

230 

i  750 

I  350 

I  890 

I  120 

stopped    application    at    Jewel 
filter 

;; 

5.00     " 

23-5 

i  290 

I  690 

I  320 

870 

850 

\  Application    of    sulphate   of    alu 

;; 

11.30    " 

23.5 

2  IIO 

2390 

I  040 
I  540 

650 

595 

" 

5.00    " 

23-5 

2  290 

2  04O 

640 

715 

302 
489 

II.  OO  P.M. 

23-5 

1950 

I  310 
I  840 

529 
610 

45i 
258 

3 

5.00     " 

23-5 

I  360 

I  250 

43° 
660 

281 
385 

3 

11.00       " 

23.5 

I  510 

1970 

339 
286 

306 

222 

3 

5.00     " 
8  oo     " 

23-5 

I  530 

I  140 

301 

254 

I78 
173 

3 

11.00       " 

23-5 

I   I/O 

I  O20 

219 

2OO 
286 

4 

5.00     " 
8  30     " 

23-5 

I  O6O 

930 

I  580 

242 

149 

191 

4 

12.00  M. 

23-5 

990 

950 

184 

319 
125 

4 

5.00     " 
8.00     " 

23-5 

970 

I  57° 

161 
151 

129 
146 

4 

11.00       " 

23-5 

8So 

i  740 

172 

99 
log 

5 

5.00     " 
8.00     " 

23-5 

860 

3  i8d 

M5 
154 

87 
in 

5 

II.  OO       " 

23.5 

650 

710 

157 
202 

95 
153 

5 

4.30    " 

23-5 

610 

840 
i  580 

167 
415 

143 
399 

7 

II.  OO       " 

23-5 

790 

890 

237 
194 

223 
181 

7 

5.00    " 

8.00     " 

23-5 

670 

870 

190 
152 

103 
141 

7 
"        8 

II.  OO       " 

23-5 

660 

I  420 

850 

144 
117 

1  08 
108 

8 
8 
8 
8 

5.00    " 

II.  OO       " 
4.30  I'.M. 

8.00     " 

23.5 
23-5 
23-5 

780 
550 
610 

910 
1970 
i  740 

93 
163 
Si  23 
118 

81 

53 
87 

g  Agitated  and  drained  water  frorr 
surface  of  sand  layer  at  1.25  P.M 

8 
9 

n.oo     " 

2.OO  A.M. 

23.5 
23-5 

610 

i  090 
i  420 

96 
97 

74 

53 

WATER   PURIFICATION  AT  LOUISVILLE. 


BACTERIA    PER    CUBIC    CENTIMETER    IN    THE    OHIO    RIVER    WATER    BEFORE    AND    AFTER 
TREATMENT    BY   THE   POLARITE   SYSTEM.— Concluded. 


Rate  of 

Filtration. 

Ba 

cteria  per  Cu 

bic  Centimete 

r. 

Dale. 

Hour. 

Cubic 
Feet  per 
Minute. 

River 
Water. 

B.2S* 

Effluent. 

Jewell 
Effluent. 

Polarite 
Effluent. 

Remarks. 

IS97 
June     9 

5.00  A.M. 

23-5 

570 

I  310 

104 

53 

9 

II.  OO       " 

23-5 

39° 

540 

88 
*84 

37 
53 

*  Agitated  and  drained  water  from 

9 

5.00       " 

23-5 

500 

640 

55 

53 

surface  of  sand  layer  at  2  oo  P.M. 

9 

I  I  .  OO       " 

23-5 

500 

510 
54O 

54 
61 

27 
33 

"         o 

5.00    " 

S  oo     " 

23-5 

510 

620 

580 

55 
t59 

53 

f  Agitated  and  drained  water  from 

"            0 

II.OO       " 

23o 

450 

97° 

49 

41 

surface  of  sand  layer  at  6.35  A.M. 

"         o 

5-30     " 

23-5 

370 

950 

*59 

47 

surface  of  sand  layer  at4.$i  I'-M. 
3  Agitated  and  drained  water  from 

"        o 

II.OO       " 

23-5 

520 

460 

§60 

lUc 

39 

surface  of  sand  layer  at  9.30  P.M. 

I 

5.00     " 
8  30     " 

230 

530 

300 

154 

27 

surface   of   sand  layer  at    12.00 

A.M. 

"         I 

II.OO       " 

2j.5 

390 

I  090 

t5i 

30 
41 

"Agitated  and  drained  water  from 
surface  of  sand  layer  at  3.00  A  M. 

"        I 
"         I 
"         I 

"            2 

5.00     " 
8.00     " 

II.OO       " 
5.OO  A.M. 

23-5 
23-5 
23-5 
23-5 

53° 

410 
390 

370 
300 
420 
370 

47 
45 
37 
41 

40 
32 
52 
43 
26 

*  Agitated  and  drained  water  from 
surface  of  sand  layer  at  7.17  A.M. 
f  Washed  Jewell   filter  from  below 
at    8.53    A.M.,    using    644    cubic 
feet  of  wash  water. 

,, 

38 

28 

"            2 

4.30       " 

23-5 

790 

490 

53 

48 

INVESTIGATIONS  Ol-    THE  WATER  COMPANY  FROM  APRIL   TO  JULY,  18U7.  333 


CHAPTER   XV. 

INVESTIGATIONS  OF  THE  WATER  COMPANY   FROM  APRIL  TO  JULY,  1897,  AND  A  RECORD 
AND  DISCUSSION  OF  THE  RESULTS  ACCOMPLISHED 
IN  CONNECTION  THEREWITH. 


TIIK  status  of  the  problem  of  the  purifica 
tion  of  the  Ohio  River  water,  for  the  water 
supply  of  the  city  of  Louisville,  on  March  10, 
1897,  when  it  was  decided  that  the  Water 
Company  should  conduct  further  investiga 
tions  along  this  line,  and  independent  of  the  ' 
companies  previously  associated  in  the  tests, 
may  he  briefly  stated  as  follows: 

i.  The  Warren,  Jewell,  Western  Gravity, 
and  Western  Pressure  Systems,  in  the  form  in 
whic'h  they  were  tested,  were  not  capable  of 
purifying  the  Ohio  River  water  in  a  practi 
cable  manner,  for  the  following  principal  rea 
sons: 

a.  The  absence  of  suitable  provisions  to  al 
low    the    suspended    matters    to    subside    by 
gravity  caused  the  use  of  coagulating  chemi 
cals  in  amounts  which  made  their  use  expen 
sive  to  an  excessive  degree,  and  which  were 
objectionable  with  regard  to  the  quality  of  the 
filtered  water. 

b.  The  absence  of  suitable  settling  basins 
to    allow    subsidence    (sedimentation)    to    be 
employed  to  its  economical  limits  caused,  at 
times  of  muddy  water  in  the  river,  so  much 
suspended  matter  to  pass  on  to  the  filter,  that 
in  at  least  one  case  the  filter  was  unable  to 
purify  enough  water  to  wash  it  properly;  and 
in  the  case  of  the  best  filters,  it   would   be 
necessary  in  practice  to  provide  reserve  fil 
ters,  with  an  area  of  65  to  75  per  cent,  of  those 
normally  in  service.    The  cost  of  construction 
and  of  operation  at  irregular,  but  unknown, 
intervals,  of  such  a  large  reserve  portion  of  a 
plant,  would  increase  the  cost  of  purification 
very  materially. 

r.  The  absence  of  suitable  settling  basins 
to  allow  subsidence  to  be  employed  to  its 
economical  limits,  would  cause,  at  times,  in 


practice  with  the  best  available  filters,  the 
wasting  of  from  25  to  35,  and  occasionally 
even  a  greater,  per  cent,  of  filtered  water,  in 
order  to  wash  the  filters  properly.  This  large 
waste  of  water  would  call  for  the  use  of  more 
pumping  machinery,  and  would  thus  increase 
the  cost  of  pumping  the  water  which  actually 
reached  the  consumers.  Furthermore,  the 
waste  of  filtered  water,  which  would  be  used 
in  washing  the  filters,  and  thence  run  into  the 
sewer,  would  mean  practically  a  correspond 
ing  waste  of  coagulating  chemicals. 

(/.  It  was  demonstrated  conclusively  that, 
owing  to  the  very  frequent  and  marked 
changes  in  the  composition  of  the  water  in 
the  Ohio  River,  it  was  difficult  to  give  to  the 
systems  of  purification  suitable  attention  to 
guard  against,  on  the  one  hand,  an  imper 
fectly  purified  effluent,  and,  on  the  other 
hand,  an  unnecessarily  large  application  of 
coagulating  chemicals,  with  its  needless  in 
crease  in  the  cost  of  chemical,  and  in  certain 
objectionable  results  in  consequence  thereof. 
With  a  proper  employment  of  subsidence, 
it  would  be  much  easier  to  operate  a  large 
system  of  purification  satisfactorily,  inde 
pendent  of  the  consideration  of  a  large  and 
needless  reserve  portion  of  the  system. 

2.  The     Harris     Magneto-electric    System 
was  a  complete  failure. 

3.  The  use  of  an  electrolytic  action  upon 
metallic  aluminum  plates,  such  as  was  tried  by 
the  Harris  Company  in  July,  1896,  and  inves 
tigated   further  by   the  Water   Company,   in 
August,  1896,  with  a  view  to  its  substitution 
for  sulphate  of  alumina,  as  a  means  of-secur- 
ing  a  coagulating  chemical,  did  not  give  prom 
ise  of  practicability,  owing  to  its  cost.     This 
method    possessed    certain   advantages   over 


334 


WATER   PURIFICATION  AT  LOUISVILLE. 


sulphate  of  alumina,  however,  as  was  pointed 
out  in  foregoing  chapters. 

4.  The  suhstitution  of  iron  plates  for  alu 
minum  plates,  in  the  electrolytic  method,  re 
duced  the  cost,  hut  the  results  obtained  in 
connection  with  the  Mark  and  Brownell  de 
vices  were  so  inadequate  that  the  practicabil 
ity  of  this  method  was  an  open  question  at 
this  time. 

>  The  results  of  laboratory  experiments 
indicated  the  advisability  of  considering  other 
coagulating  chemicals  than  sulphate  of  alu 
mina,  notably  the  iron  compounds. 

In  cor.nection  with  the  importance  of  the 
last  mentioned  point,  it  may  be  added  that 
the  results  of  the  experiments  in  1884,  and  of 
more  recent  observations,  indicated,  but  did 
not  prove  conclusively,  that,  after  the  removal 
of  coarse  particles  by  plain  subsidence,  the 
Ohio  River  water  would  require,  at  times, 
coagulation  and  further  subsidence  before 
economical  filtration,  either  by  the  English  or 
American  type  of  filters,  could  be  adopted. 
As  was  stated  in  the  last  chapter,  it  was  de 
cided  shortly  before  this  time  to  test  the 
polarite  system,  in  which  it  was  claimed  that 
no  use  was  made  of  chemicals.  It  was  learned, 
however,  before  these  investigations  were 
half  completed,  that  this  last  system  was  im 
practicable. 

OBJECTS  OF  THE  INVESTIGATIONS. 

The  objects  of  the  investigations  were  to 
obtain  practical  information,  so  far  as  was 
possible  on  an  experimental  scale,  and  with 
appliances  which  could  be  made  promptly 
available,  on  the  following  principal  points: 

1.  The  removal  of  mud,  silt,  and  clay  from 
the  river  water  by  plain  subsidence  (i.e..  un 
aided  by  coagulating  chemicals). 

2.  The  relative  economy,  advantages,  and 
disadvantages    of    all    available    coagulating 
chemicals,     prepared     by     various     methods 
(chemical  and  electrolytical). 

3.  The  most  economical  and  efficient  ap 
plication  of  coagulating  chemicals  to  aid  in 
the  removal  of  the  bulk  of  various  suspended 
matters  by  subsidence. 

4.  The  most  economical  and  efficient  ap 
plication  of  coagulating  chemicals,  to  aid  in 
the    rapid    filtration    of    the    water,    follow 


ing  a  partial  purification  by  preliminary  sub 
sidence. 

5.  The  consideration  of  the  best  method  of 
grouping  together  the  available  information 
upon  the  foregoing  [joints,  with  the  view  to 
determining  the  system  of  purification  which 
would  give  at  a  minimum  cost,  an  effluent  of 
the  best  quality  from  a  practical  point  of 
view. 

PLAN  OK  PRESENTATION  OF  THE  RESULTS  OF 

Til  KSE     1  NVKSTIGATIONS. 

There  were  two  principal  lines  of  evidence 
obtained  during  these  investigations.  The 
major  portion  came  from  experiments  made 
with  a  series  of  devices,  including  settling 
basins,  electrical  and  other  appliances,  for  the 
preparation  and  application  of  different  co 
agulating  chemicals,  and  also  the  Je\vell  filter. 
Additional  data  of  importance  were  also  ob 
tained  from  laboratory  experiments,  and  from 
the  separate  operation  of  portions  of  the 
above-mentioned  series  of  devices,  notably 
those  for  the  electrolytic  production  of  co 
agulating  chemicals. 

The  plan  adopted  for  the  presentation  and 
discussion  of  the  results  of  these  investiga 
tions  is  as  follows: 

A  description  is  first  given  of  the  devices 
which  were  employed.  The  conditions  under 
which  these  devices  were  operated  are  next 
described.  A  detailed  record  of  the  results 
of  analyses  is  then  presented,  followed  by  a 
summary  of  all  the  principal  data  obtained 
from  the  operation  of  these  devices. 

The  remaining  portion  of  the  chapter,  con 
taining  a  discussion  upon  various  points  di 
rectly  related  to  the  above-stated  objects  of 
the  investigations,  is  of  most  importance.  In 
it  use  is  made  of  such  portions  of  the  sum 
mary  which  precedes  it  as  bear  upon  the  point 
in  q-uestion;  and  the  results  of  the  laboratory 
and  other  special  experiments  are  recorded  in 
their  appropriate  place  in  the  discussion. 

It  will  be  noted  that,  at  the  close  of  each 
section  of  the  discussion,  conclusions  are 
drawn,  so  far  as  the  available  information 
upon  the  point  in  question  will  permit.  These 
conclusions,  with  those  from  other  portions 
of  the  report,  are  grouped  together  as  a  mat 
ter  of  convenience  in  Chapter  XVI. 


INVESTIGATIONS  OF  THE   WATKR  COMPANY  FROM  APRIL   TO  JULY,  1897.  335 


DESCRIPTION    OF   THE    DEVICES   ARRANGED 

AND  OPERATED  BY  THE  WATER 

COMPANY. 

For  the  purpose  of  carrying  on  investiga 
tions  along  the  several  lines  referred  to  above, 
use  was  made  in  so  far  as  possible  of  appar 
atus  and  devices  available  at  the  pumping 
station.  Supplementary  devices  were  de 
signed  of  such  style  and  construction  as 
would  be  convenient  in  carrying  on  this  work 
without  prolonged  delays  for  construction, 
and  at  the  same  time  conform  to  the  arrange 
ment  of  devices  already  at  hand. 

In  order  to  make  the  results  of  operation 
comparable  with  those  of  earlier  work,  the 
system  was  arranged  to  be  operated  on  a  basis 
of  250,000  gallons  per  24  hours  (23.2  cubic 
feet  per  minute),  as  was  the  case  with  the 
other  systems  investigated.  Except  for  the 
purpose  of  comparing  the  effects  of  different 
rates  of  filtration,  and  in  some  cases  of  in 
creasing  the  amount  of  electrolytic  treatment, 
this  rate  was  maintained  as  nearly  as  possible. 

The  full  system  of  devices,  which  were  in 
use  wholly  or  in  part  during  these  investiga 
tions,  included  the  following: 

1.  Two    circular   wooden    tanks    of    about 
4000  and   1000  cubic  feet  capacity,  respect 
ively.      These    were    used    as    settling    (sub 
sidence)  basins. 

2.  Four  wooden  tanks  of  about  400  gallons 
capacity  each,  for  the  preparation  of  chemi 
cal  solutions. 

3.  One  electric  generating  plant,  consist 
ing  of  a  5O-H.P.  steam-engine,  and  a  2O-kilo- 
watt  dynamo.     (See  Chapter  XIII.) 

4.  Four  electrolytic  cells  for  the  prepara 
tion     of    coagulants     electrolytically.       (See 
Chapters  X  and  XIII.) 

5.  Four  sets  of  metal  electrodes,   two   of 
iron  and  two  of  aluminum. 

6.  The  settling  chamber  and  filter  of  the 
Jewell  System  of  purification.     (See  Chapters 
IV  and  V.) 

7.  Necessary    pumps,    piping,    valves,    and 
meters,  to  allow  the  desired  operations  and 
observations. 

This  system  of  devices,  or  portions  thereof, 
was  arranged  at  various  times  in  a  manner 
to  permit  several  different  ways  of  operation, 
as  indicated  below: 


1.  River  water  was  admitted  directly  to  the 
inlet    of    the    Jewell    settling    chamber;    and 
various  coagulants  were  applied  at  the  inlet  or 
the  outlet  of  this  chamber,  as  desired. 

2.  River  water  was  admitted  at  the  bottom 
of  the  large   basin    (basin    No.    i),   removed 
from  the  top  of  this  basin,  and  pumped  into 
the  bottom  of  basin  No.  2.    Thence  it  was  re 
moved   from    the   top    of   basin    No.    2,   and 
pumped    into    the    Jewell    settling    chamber. 
Different  coagulants  were  applied  at  the  inlet 
to  basin  No.  2,  and  the  inlet  to  the  Jewell 
settling   chamber,    or   at    only   one    of   these 
places,  as  desired. 

3.  In  this  case  the  use  of  basin  No.  2  was 
omitted,    and    the    water   passed    from    basin 
No.  i  directly  to  the  Jewell  settling  chamber. 
Coagulants  were  applied  at  the  inlet  to  basin 
No.    i   (chemicals  only),  and  at  the  inlet  or 
outlet  of  the  Jewell  settling  chamber,  as  de 
sired. 

A  more  detailed  description  of  the  various 
devices  is  next  presented. 

Settling  Basins. 

Basin  No.  i. — This  was  a  circular  pine 
tank,  placed  in  the  house  formerly  occupied 
by  the  Western  Systems,  and  had  the  follow 
ing  inside  dimensions:  Diameter  at  the  bot 
tom,  17.0  feet;  diameter  at  the  top,  10.33 
feet;  and  height,  19.0  feet.  Its  total  capacity, 
and  average  working  capacity  were  4110  and 
4000  cubic  feet,  respectively.  The  staves 
and  the  bottom  of  the  tank  were  3  inches 
in  thickness.  It  was  held  together  by  13 
iron  bands,  varying  in  width  from  4  inches 
to  2  inches,  and  each  0.125  inch  thick.  The 
lowest  band  was  at  the  bottom  of  the  tank, 
and  above  it  the  successive  bands  were  placed 
at  distances  apart  increasing  from  i  foot  at 
the  bottom  to  3  feet  at  the  top. 

The  4-inch  inlet  pipe  entered  at  the  side. 
about  2.5  feet  above  the  bottom,  and  extended 
into  the  tank  a  distance  of  about  8  feet.  The 
flow  of  water  was  regulated  by  a  gate  valve 
placed  on  the  inlet  pipe  outside  the  tank,  sup 
plemented  by  a  single-seated  check  valve,  op 
erated  by  a  float  on  the  inside  of  the  tank.  In 
front  of  the  mouth  of  the  inlet  pipe,  which  lay 
horizontally,  was  a  small  baffle  plate,  distant 
about  3  inches,  arranged  with  the  view  to 


136 


WATER   PURIFICATION  AT  LOUISVILLE. 


breaking  the  current  of  water.  The  4-inch 
outlet  pipe  was  connected  to  the  tank  about 
J  5  inches  from  the  top,  and  on  the  same  side 
as  the  inlet  pipe. 

Connections  were  made  for  draining  into 
the  sewer  through  an  8-inch  opening  in  the 
bottom  of  the  tank  at  one  side.  During  op 
eration  this  opening  to  the  sewer  was  closed 
by  a  plug.  The  bottom  of  the  tank  was  nearly 
level,  and  it  was  necessary  to  use  a  stream  of 
water  from  a  hose,  and  a  broom,  to  remove 
the  accumulation  of  sediment. 

Applications  of  aniline  dyes,  and  of  caustic 
soda,  were  made  to  the  water  as  it  entered  the 
basin,  and  tests  were  made  to  note  the  appear 
ance  of  the  chemicals  at  the  outlet.  The  re 
sults  of  these  tests,  to  learn  the  way  in  which 
the  water  passed  through  this  basin,  are  sum 
marized  just  beyond,  together  with  cor 
responding  results  from  the  other  settling 
basins. 

Basin  No.  2. — This  basin  was  made  by  re 
pairing  the  tank  formerly  used  as  the  West 
ern  gravity  filter.  (See  Chapter  V.)  The 
inside  dimensions  were  as  follows:  Diameter 
at  the  bottom,  10.0  feet;  diameter  at  the  top, 
9.5  feet;  and  height,  14.0  feet.  Its  total  ca 
pacity,  and  average  working  capacity  were 
1045  and  looo  cubic  feet,  respectively. 

The  4-inch  inlet  pipe  was  connected  to  the 
side  of  the  tank  by  a  flange  joint,  2.0  feet 
above  the  bottom.  A  4-inch  pipe,  which  was 
connected  to  the  tank  on  the  opposite  side 
from  the  inlet,  and  2.5  feet  below  the  top, 
formed  the  outlet.  There  were  no  baffle 
plates  or  other  devices  in  this  tank  to  assist 
in  making  uniform  the  displacement  of  water. 
A  3-inch  pipe  was  connected  to  an  opening 
in  the  bottom,  to  allow  drainage  to  the  sewer. 
The  sediment  on  the  bottom  was  removed 
by  a  stream  of  water  from  a  hose  and  by  a 
broom. 

The  results  of  the  application  of  chemicals 
to  the  water,  in  ordej  to  learn  the  manner 
in  which  the  water  passed  through  this  basin, 
are  summarized  beyond,  with  corresponding 
results  from  the  other  basins. 

Jewell  Settling  Chamber.  —  This  chamber 
has  already  been  described  in  full  in  Chapter 
IV.  It  was  a  closed  compartment  cylindri 
cal  in  form,  6.79  feet  high  and  13.5  feet  in 
diameter,  inside  dimensions,  having  a  capac 


ity  of  879  cubic  feet.  It  was  used  without 
modifications  in  all  operations  up  to  June  19. 
On  this  date  wooden  boxes  were  inserted  to 
cover  the  portions  of  the  inlet  and  outlet 
pipes  lying  within  the  chamber.  The  end  of 
the  inlet  pipe  was  enclosed  in  a  box,  so  that 
the  water  entered  the  chamber  at  the  bottom 
instead  of  1.55  feet  above  the  bottom  as  for 
merly,  as  the  sides  and  front  of  the  box  were 
3  inches  above  the  floor  of  the  chamber.  By 
means  of  wooden  framing  the  outlet  pipe  (at 
the  top  of  the  chamber)  was  closed  in,  leaving 
an  opening  6  inches  wide  and  24  inches  long, 
about  diametrically  opposite  to  the  inlet  pipe. 
The  water  passed  through  this  opening  into 
the  portion  enclosed  by  the  wooden  parti 
tions,  and  thence  to  the  filter,  by  means  of  the 
regular  central  pipe  which  served  as  an  out 
let  to  the  settling  chamber. 

The  results  of  the  application  of  chemicals 
to  the  water  (after  the  above  stated  modifica 
tion  was  made),  in  order  to  learn  the  manner 
in  which  the  water  passed  through  the  cham 
ber,  arc  summarized  in  the  next  table,  to 
gether  with  corresponding  results  from 
basins  Nos.  i  and  2. 

TABLE  SHOWING  A  SUMMARY  OF  THE  RESULTS 
OF  THE  TESTS  OF  THE  DISPLACEMENT  OF 
WATER  ON  ITS  PASSAGE  THROUGH  SETTLING 
BASINS  NOS.  1  AND  2.  AND  THE  JEWELL 
SETTLING  CHAMBER. 


Normal  capacity  in  cubic  feet 4  ooo       I  coo      879 

Time    of   filling   at  the    regular   rale 

(23.2  cubic  feet  per  minute) !2h.  52m.    43m.      3Sm. 

Time   elapsing   between    applirationj 

of  chemicals  at   the  inlet  and  first 

appearance  at  the  outlet 3gm.         4m. 

Time  elapsing  between    application| 

of  chenvcals  at  the  inlet  and  max-; 

imum  appearance  at  the  outlet.. ..  ih.  lorn.     lorn. 
Percentage  which  chemical  appearing 

at  the  end  of  "time  of  filling"  was, 

of  maximum  which  appeared   ....        24  33 

Time   elapsing   between   application 

of     chemicals    at     the     inlet    and 

appearance  of  50  per  cent,  at  the 

outlet 2h.  4gm.    3Om. 


Application   of   Chemical   Solutions   to    Secure 
Coagulation. 

For  preparing  chemical  solutions  four 
wooden  tanks,  each  of  about  400  gallons 
capacity,  were  used.  They  were  arranged  in 


INVESTIGATIONS  OF  Till'.    M'ATKR  COMPAXY  FROM  APRIL   TO  JULY,  M>7.  337 


pairs,  one  above  the  other,  and  the  corre 
sponding  upper  and  lower  tanks  were  used 
for  the  same  kind  of  chemicals.  Solutions 
were  prepared  in  the  upper  tanks,  and  ad 
mitted  to  the  corresponding  lower  tanks  as 
required,  the  lower  tanks  serving  for  pump 
wells  and  storage  basins. 

Pumps. — In  addition  to  the  small  pump 
used  by  the  Jewell  Company  in  1895-96  (de 
scribed  in  Chapter  11),  a  small  duplex  pump, 
having  the  following  principal  dimensions, 
was  placed  in  operation:  Diameter  of  steam 
cylinder.  1.125  inches;  diameter  of  water  cyl 
inder,  2  inches;  length  of  stroke,  2.75  inches. 

Piping. — Each  pump  was  provided  with 
two  suction  pipes,  0.75  inch  in  diameter, 
which  reached  to  within  i  inch  of  the  bottom 
of  the  lower  tanks.  By  this  arrangement  the 
pumps  could  be  supplied  with  solution  from 
either  tank.  For  delivery  pipes,  use  was 
made  of  such  small  piping  as  was  available 
at  the  pumping  station.  In  the  case  of  the 
old  (simplex)  pump,  the  o.75-inch  heavy  lead 
pipe  used  in  the  Jewell  System  was  utilized. 
It  was  connected  to  the  inlet  pipe  of  the  set 
tling  chamber,  at  a  point  about  6  feet  from 
the  chamber,  or  lowered  about  3  feet  into  the 
pipe  leading  from  the  top  of  the  settling 
chamber  to  the  filter,  as  it  was  desired  to  ap 
ply  the  chemicals  before  or  after  the  water 
had  passed  through  the  settling  chamber,  re 
spectively.  The  delivery  pipe  from  the  new 
(duplex)  pump  was  connected  to  the  inlet  to 
basin  No.  i.  or  to  the  inlet  to  basin  No.  2, 
as  desired.  It  was  mainly  made  up  of  0.5- 
inch  iron  pipe,  but  for  connection  to  the  inlet 
to  basin  No.  i  about  40  feet  of  o.75-inch 
iron  pipe  were  also  used. 

Kinds  of  Chemicals. — In  connection  with 
the  operation  of  the  devices  under  considera 
tion  five  different  chemicals,  as  follows,  were 
used  at  various  times: 

1.  Sulphate  of  alumina  (two  different  lots). 

2.  Persulphate  of  iron. 

3.  Potash  alum. 

4.  Protosulphate  of  iron  (copperas). 

5.  Caustic  soda. 

A  number  of  other  chemicals  were  used  in 
laboratory  experiments,  as  will  appear  in  a 
subsequent  portion  of  this  chapter. 

The  composition  of  the  above  chemicals 
is  given  in  the  next  section.  No  special 


features  are  to  be  noted  here,  except  in  the 
case  of  the  persulphate  of  iron.  In  making 
solutions  (from  0.3  to  0.9  per  cent.,  accord 
ing  to  the  quantity  to  be  applied)  of  this 
chemical  in  filtered  water,  it  was  difficult  to 
dissolve  it.  It  was  found,  however,  that  a 
solution  could  be  made  best  by  adding,  suc 
cessively,  small  quantities  of  water  to  the  sub 
stance  at  the  outset,  and  decanting  the  solu 
tion  into  another  tank.  Hot  water  could  not 
be  used,  because  it  decomposed  the  chemical. 
and  with  cold  water  there  was  also  a  tend 
ency  for  the  iron  to  form  the  sticky  hydrate, 
which  retarded  the  solution  of  the  portion 
covered  by  it.  This  chemical  contained 
considerable  material  which  was  completely 
insoluble  (see  the  analysis  below),  and  it 
was  necessary  to  remove  this  by  straining 
through  cloth,  because  it  cut  the  fittings  of 
the  pumps  and  meters.  There  was  also 
enough  free  sulphuric  acid  (2.73  per  cent.)  in 
the  persulphate  of  iron  to  corrode  the  brass 
and  iron  pipes  and  fittings  very  rapidly.  It 
is  possible,  however,  to  obtain  a  commercial 
product  of  this  kind  which  does  not  possess 
these  disadvantages,  except  perhaps  a  small 
amount  of  insoluble  matter. 

Tn  the  case  of  the  potash  alum,  which  con 
tained  a  small  quantity  of  ammonia,  all  quan 
tities  are  calculated,  as  was  the  case  in  1896, 
as  sulphate  of  alumina,  on  the  basis  that  six 
teen  parts  of  the  former  equal  ten  parts  of  the 
latter. 

Composition  of  Chemicals. — The  two  lots  of 
sulphate  of  alumina,  and  the  lot  of  persul 
phate  of  iron,  were  analyzed  with  the  follow 
ing  results: 

PERCENTAGE   COMPOSITION   OF   COAGULATING 
CHEMICALS. 


Sulphate  o 

f  Alumina. 

Petsul- 

I.o,  No., 

Mailer  insoluble  in  waler  
Available  alumina  (A1>O,)  
Sulphuric  acid  (SO,)  

0.22 
15.96 

34  •  26 

0.06 
19.64 

36.85 

5-56 

o.oo 
55.08 

Oxkle  of  iron  (FejOi)  

o.oo 

Trace 

I  ime  (CaO)   

0.56 

0.06 

o  .  oo 

Water  (H?O)                    

49.00 

43  •  39 

4.46 

The  potash  alum  was  of  high  grade  and 
had  about  10.7  and  34.0  per  cent,  of  alumina 
and  sulphuric  acid,  respectively. 

The  copperas  crystals  were  also  of  a  good 
quality,  and  contained  57.55  and  28.78  per 


338 


WATER^P  UNIFICATION  AT  LOUISVILLE. 


cent,   of  iron   oxide  and   sulphuric  acid,   re 
spectively. 

Analyses  of  the  caustic  soda  showed  that 
it  contained  73.4  per  cent,  of  sodium  oxide. 

Devices    for    the    Application    of    Electrolytic 
Treatment  to  Secure  Coagulation. 

Two  electrolytically  prepared  coagulants 
(hydrate  of  aluminum  and  hydrate  of  iron) 
were  used  at  various  times.  Each  was  pre 
pared  by  the  electrolytic  decomposition  of 
electrodes  of  the  respective  metal.  For  the 
purpose  of  preparing  these  hydrates,  elec 
trodes  in  the  form  of  manifolds  of  plates  were 
placed  in  closed  iron  cells,  and  the  river  water 
and  electric  current  passed  through  them. 
The  following  devices,  all  of  which  were 
placed  in  the  house  formerly  occupied  by  the 
Warren  System,  were  used: 

Generating  Plant. — The  electric  generating 
plant  used  in  connection  with  the  Mark  and 
Brownell  devices  was  employed  for  genera 
ting  the  necessary  electric  current. 

The  dynamo  was  rated  at  400  amperes  and 
50  volts,  but  could  be  operated  as  high  as 
450  amperes  safely  for  short  periods.  For 
a  full  description  of  this  engine  and  dynamo 
see  Chapter  XIII.  As  already  described,  the 
electric  current  was  regulated  by  means  of  a 
field  rheostat.  In  order  to  maintain  the  re 
sistance  necessary  to  balance  the  potential  of 
the  machine,  when  operating  with  low  am 
perage,  a  large  rheostat  was  inserted  on  the 
main  circuit.  At  the  close  of  these  investi 
gations,  Aug.  i,  1897,  tests  were  made  of  the 
engine  and  dynamo,  with  the  following  re 
sults: 

RESULT   OF  TESTS   OF   ELECTRIC    GENERATING 
PLANT. 

ENGINE  TEST. 


Kffic 


Indi 


50 

37-5 
25.0 

12  .O 


DYNAMO  TKST. 


95  per  cent. 
Q3 

85        " 
70 

Urake  Horse  Po 


Owing  to  the  fact  that  the  engine  (50 
I.H.P.)  was  a  much  larger  machine  than  the 
dynamo  (28  E.H.P.),  and  was  accordingly 
at  all  times  operated  considerably  below  the 
point  of  maximum  efficiency;  and,  further, 
owing  to  the  fact  that  at  times  the  entire 
plant  was  too  large  to  give  economically  the 
small  amount  of  electric  power  required  for 
the  treatment  of  fairly  clear  water,  the  com 
bined  efficiency  of  the  engine  and  dynamo 
was  very  low  in  some  cases.  In  practice, 
however,  a  generating  plant  would  be  ar 
ranged  in  several  units,  and  such  portions  of 
it  used  as  would  furnish  the  electric  current 
most  economically.  Under  such  circum 
stances  the  above  tests  show  that  80  per  cent. 
of  the  indicated  horse  power  at  the  engine 
could  be  obtained  as  electric  power.  This 
agrees  fairly  well  with  the  results  of  good 
I  modern  practice. 

Electrolytic  Cells. — Four  electrolytical  cells, 
j  with  covers,  were  used  in  this  work.  Cells 
Nos.  i  and  2  were  those  of  the  Mark  and 
Brownell  devices,  and  have  been  fully  de 
scribed  in  Chapter  XIII.  Cells  Nos.  3  and 
4  were  two  of  the  large  cells  of  the  Harris 
Company,  with  whom  arrangements  for  their 
use  were  made.  These  cells  have  been  de 
scribed  in  Chapter  X.  Several  changes  in 
all  of  these  cells  were  made,  as  follows: 

Changes  in  Cells  Nos.  i  and  2. — These  du 
plicate  cells  were  30  inches  in  diameter,  had 
a  capacity  of  35.2  cubic  feet,  and  were  not 
insulated  on  the  inner  walls.  The  special 
distributing  devices,  attached  to  the  inner 
side  of  the  dome  at  the  top,  were  removed, 
and,  in  each  case,  the  4-inch  inlet  pipe  was 
connected  by  a  flange  joint  to  the  center  of 
the  dome-shaped  cover.  The  original  out- 
lets  on  the  side  were  closed  by  plugs,  and 
the  3-inch  opening  at  the  apex  of  the 
conical  bottom  in  each  cell  was  used  as  an 
outlet. 

Changes  in  Cells  Nos.  j  and  4. — These  du 
plicate  cells  were  removed  from  the  Harris 
house  to  a  position  by  the  side  of  cells  Nos. 
i  and  2.  They  were  35.5  inches  in  diameter, 
and  had  a  capacity  of  28  cubic  feet.  The  in 
sulating  rubber  linings,  and  the  covers  of  a 
special  casting,  with  magnets  resting  upon 
them,  were  removed.  A  slightly  arched  and 
circular  iron  plate,  to  which  the  4-inch  inlet 


INVESTIGATIONS  OF  THE   WATER  COMPANY  FROM  APRIL   TO  JULY,  1897.  339 


pipe  was  attached  in  the  center,  served  as  a 
cover  in  each  case.  A  wooden  frame  was 
built  in  the  bottom,  so  that  the  electrodes 
when  placed  upon  it  reached  within  0.25  inch 
of  the  flange  to  which  the  cover  was  attached. 
There  was  tapped  in  each  cover  a  hole,  to 
which  a  o.25-inch  pipe,  with  a  pet-cock,  was 
attached,  in  order  to  allow  the  escape  from 
time  to  time  of  accumulated  gases.  The  3- 
inch  opening  in  the  bottom  of  the  cone  was 
connected  with  a  4-inch  pipe,  which  served 
as  an  outlet  and  waste  pipe. 

Electrodes. — New  electrodes,  numbered  the 
same  as  the  cells  in  which  they  were  placed, 
were  constructed,  and  used  exclusively  in  the 
tests  described  in  this  chapter.  Electrodes 
Nos.  i  and  3  were  each  made  of  a  manifold 
of  wrought-iron  plates  o.  125-inch  thick. 
Electrodes  Nos.  2  and  4  were  made  of  alu 
minum,  to  duplicate  Nos.  i  and  3. 

In  the  method  of  construction  these  four 
electrodes  were  identical.  The  "size  of  the 
cells  used  necessitated  slightly  different 
forms,  however.  Each  manifold  contained 
fifty-six  plates. 

Size  of  Plates. — Electrodes  Nos.  I  and  2 
were  made  of  plates  50  inches  long.  In  or 
der  to  fit  the  cell  the  widths  of  the  plates 
varied  from  24  to  12  inches,  averaging  20.4 
inches.  The  total  area  of  one  side  of  the 
plates  was  56,000  square  inches,  and  the  cross 
section  of  the  electrolyte  was  55,400  square 
inches.  When  new,  these  sets  of  plates 
weighed  1780  and  674  pounds,  respectively. 
Electrodes  Nos.  3  and  4  were  made  of  plates 
36  inches  long.  The  widths  varied  from  30 
to  22  inches,  and  averaged  27.4  inches.  The 
total  area  of  one  side  of  these  plates  was 
56,200  square  inches,  and  the  cross  section 
of  the  electrolyte  was  55.500  square  inches. 
When  new,  these  sets  of  plates  weighed  1824 
and  682  pounds,  respectively. 

Formation  of  Manifolds. — All  of  the  four 
manifolds  were  formed  alike.  The  plates 
were  held  together  by  six  i-inch  iron  bolts, 
and  the  desired  distance  between  the  plates, 
0.25  inch,  was  maintained  by  the  use  of  wash 
ers,  or  separators.  These  bolts  were  set  as 
far  to  the  edge  of  the  sets  as  the  width  of  the 
outer  plates  would  allow.  The  plates  were 
so  thin,  however,  that  they  buckled  badly, 
and  it  was  necessary  to  insert  many  small 


pieces  of  insulating  material  between  them  at 
different  places.  In  order  to  relieve  this  diffi 
culty  to  some  extent,  o. 5-inch  bolts  with 
separators. were  placed  in  the  corners  of  the 
electrodes,  at  the  same  time  that  the  other 
changes  were  made,  and  which  were  com 
pleted  May  30. 

One  of  the  upper  corners  of  each  plate  was 
cut  off,  and  the  plates  arranged  in  the  mani 
fold  so  that  the  cut  and  uncut  corners  came 
alternately  on  each  side.  To  the  uncut  cor 
ners  on  each  upper  side  brass  lugs  were 
riveted.  The  cables  carrying  the  electric 
current  were  soldered  to  these  lugs. 

Extensions  of  six  of  the  plates  of  each  set, 
with  openings  which  coincided  along  the  cen 
ter  line,  were  arranged  as  lifting  lugs  to  aid 
in  handling  the  electrodes.  When  placed  in 
the  cells  the  electrodes  rested  upon  a  wooden 
framework  arranged  in  the  bottom.  The 
space  between  the  edge  of  the  plates  and  the 
uninsulated  inner  wall  of  the  cell  ranged 
from  0.5  to  3  inches,  and  averaged  about  2 
inches.  The  outer  portion  of  the  frame 
work  at  the  bottom  was  solid,  so  that  there 
was  no  opportunity  for  water  to  pass  down 
ward  through  a  cell,  except  through  the 
spaces  between  the  plates  of  the  electrodes. 

Insulation  of  Electrodes. — Owing  to  inabil 
ity  to  secure,  without  long  delay,  hard  rubber 
fittings  for  the  insulation  of  the  electrodes,  it 
was  decided  to  proceed  as  follows: 

The  iron  bolts  by  which  the  manifold  of 
plates  was  held  together  were  covered  with 
steam  hose,  and  circular  separators  of  vul 
canized  fiber  0.25  inch  thick  were  placed  on 
the  bolts  between  each  pair  of  adjoining 
plates.  This  method  of  insulation  proved  to 
be  a  failure,  owing  to  a  certain,  but  not  ac 
curately  known,  portion  of  the  current  pass 
ing  through  the  cell  on  the  fittings.  This 
portion  of  the  current  was  consequently 
wasted,  so  far  as  the  treatment  of  the  water 
is  concerned,  and  the  greater  part  of  the  re 
sults  obtained  with  these  devices  during  the 
month  of  April,  is  of  very  little  or  no  value. 
The  cause  of  this  failure  was  the  presence  of 
small  particles  of  metal  in  the  hose  or  the 
fiber,  or  both.  An  arc  was  probably  formed 
between  the  plates,  and  the  metallic  particles 
and  molten  metal  were  deposited  in  the  inter 
vening  space.  Repeated  attempts,  with  only 


34° 


WATER    PURIFICATION   AT  LOUISVILLE. 


partial  success,  were  made  to  remedy  these 
difficulties  by  the  liberal  use  of  insulating 
tape  and  paint  on  the  hose,  and  the  removal 
and  repair  of  fibers  showing  evidence  of 
metallic  particles.  Wooden  bolts  were  also 
substituted  for  the  iron  ones.  But,  as  the 
electrodes  continued  in  service,  it  was  found 
that  the  vulcanized  fiber  separators  absorbed 
water  so  that  they  swelled  to  a  degree  that 
caused  the  electrodes  to  lose  their  original 
form,  and  stripped  off  the  heads  of  the 
wooden  bolts.  During  the  first  week  in  May 
it  was  decided  to  abandon  the  original  insu 
lating  appliances,  and  procure  an  entire  set 
of  hard  rubber  fittings  to  cover  the  iron  bolts, 
and  to  separate  the  plates.  On  the  large 
bolts  the  new  separators  were  3  inches  in 
diameter,  and  on  the  small  bolts.  2  inches. 
These  changes,  which  proved  to  be  thor 
oughly  satisfactory,  were  completed  on  May 
30.  In  the  modified  form  the  fittings 
weighed  about  the  same  for  each  set,  84 
pounds. 

Electrical  Connections. — The  main  electrical 
circuit  was  the  same,  for  the  most  part,  as  in 
the  case  of  those  devices  described  in  Chapter 
XIII.  Near  the  switchboard  there  was 
placed  a  rheostat,  by  which  the  current  pass 
ing  through  the  cells  could  be  more  satisfac 
torily  regulated.  The  circuit  was  arranged 
so  that  any,  or  all.  of  the  cells  could  be  con 
nected  at  once,  and  the  direction  of  the  cur 
rent  through  any  of  the  cells  could  be 
promptly  reversed. 

Connections  with  the  electrodes  in  cells 
Xos.  I  and  2  were  made  through  two  open 
ings  filled  with  wooden  plugs,  through  which 
iron  binding  posts  were  driven.  The  main 
circuit  was  connected  to  the  outer  binding 
posts,  and  to  the  inner  binding  posts  the 
cables  attached  to  the  lugs  riveted  to  alter 
nate  plates  were  connected.  Similar  arrange 
ments  were  made  for  connecting  the  main 
circuit  with  the  electrodes  in  cells  Xos.  3  and 
4.  except  that  the  connection  through  the 
openings  in  the  cells  were  brass  binding 
posts,  placed  in  hard  rubber  stuffing  boxes. 

Modification  of  Electrode  No.  I. — In  order 
to  give  greater  treatment  to  the  water  than 
the  original  form  allowed,  electrode  Xo.  i 
was  changed,  on  July  9,  into  two  electrodes 


in  series.  This  was  accomplished  by  divid 
ing  the  set  in  halves,  electrically,  and  con 
necting  one-half  of  the  plates  on  one  side  to 
half  of  the  plates  on  the  diagonally  opposite 
side.  Xo  changes  were  made  other  than  in 
the  wiring,  as  described. 

r/ping. — As  the  iron  electrodes  (Xos.  I 
and  3)  were  never  used  in  connection  with 
the  filter  at  the  same  time  as  the  aluminum 
electrodes  (XTos.  2  and  4),  the  inlet  and  out 
let  pipes  of  each  pair  of  cells  (Xos.  i  and  2 
and  Xos.  3  and  4)  were  branches  of  the  same 
main  pipe,  respectively.  The  inlet  and  outlet 
pipes  were  4  inches  in  diameter,  except  that 
the  outlet  pipes  were  reduced  to  3  inches  at 
the  connections  with  the  cells.  Further,  the 
outlet  pipe  of  each  cell  was  itself  branched,  so 
that  by  suitable  valves  and  pipe  connections 
it  could  also  serve  as  a  waste  pipe  to  the 
sewer. 

When  basin  Xo.  T  was  in  service  the  water 
as  it  left  that  basin  could  be  pumped  through 
either  cell  Xo.  3  or  cell  XTo.  4,  on  its  way  to 
basin  Xo.  2.  Similarly,  as  the  water  was 
pumped  from  basin  Xo.  2  to  the  Jewell  set 
tling  chamber,  it  could  pass  through  either 
cell  Xo.  i  or  cell  Xo.  2.  Cells  Xos.  3  and  4 
could  not  be  used  when  basins  Xos.  i  and  2 
were  out  of  service.  At  such  times  river 
water  could  be  taken  from  the  old  Warren 
inlet  pipe  (after  slight  changes)  and  passed 
through  either  cell  Xo.  T  or  cell  Xo.  2.  on 
its  way  to  the  Jewell  settling  chamber.  Dur 
ing  the  last  of  the  tests,  after  July  9,  the 
piping  was  arranged  so  that  the  water  could 
be  pumped  from  basin  Xo.  I  through  cither 
cell  Xo.  3  or  4.  and  then  through  Xo.  i  or  2 
to  the  Jewell  settling  chamber.  A  further 
modification  at  this  time,  as  stated  above,  al 
lowed  the  passage  of  river  water  from  the  old 
Warren  inlet  directly  through  cell  Xo.  I  or 
Xo.  2,  and  to  the  Jewell  settling  chamber. 

When  chemical  solutions  were  applied  to 
the  water  prior  to  filtration,  by-passes  and 
valves  made  the  electrical  appliances  inde 
pendent  of  the  other  devices.  At  such 
times  special  experiments  were  usually  made 
with  these  appliances,  and  water  for  that  pur 
pose  was  taken  from  the  main  through  the 
old  Warren  inlet  pipe,  located  by  the  side  of 
cell  Xo.  i. 


INVESTIGATIONS  OF  THE   WATER  COMPANY  FROM  APRIL   TO  JULY,  1M7.    341 


The  Jewell  Filter. 

It  was  arranged  with  the  O.  If.  Jewell  Fil 
ter  Company  to  make  use  of  the  Jewell  filter, 
which  was  the  only  one  remaining  at  the 
pumping  station.  Xo  modifications  were 
made  in  this  filter,  which  has  been  fully  de 
scribed  in  Chapter  V. 

Pipes,  Valves,  Pumps,  and  Meters. 

From  the  foregoing  account  of  the  ways  in 
which  the  several  devices  could  be  connected, 
a  general  idea  may  be  obtained  as  to  the  ar 
rangement  of  the  piping.  Further  details  are 
not  of  importance.  But  it  may  be  recalled 
here  that  a  majority  of  the  piping  was  4 
inches  in  diameter.  A  small  portion  was  5 
inches,  and  for  a  short  distance  from  the  out 
lets  of  the  electrolytical  cells  the  diameter  was 
3  inches.  Suitable  valves,  meters,  and 
gauges  were  placed  where  convenience  re 
quired. 

Owing  to  the  fact  that  the  elevation  of  the 
Jewell  filter  was  very  nearly  as  high  as  that 
of  basins  Xos.  i  and  2,  and  that  the  water 
passed  through  some  350  feet  of  old  pipe, 
with  quite  a  number  of  turns,  valves,  meters, 
and  electrodes,  it  was  necessary  to  set  up 
pumps  on  the  pipe  between  basins  Xos.  i  and 
2  and  basin  Xo.  2  and  the  Jewell  System. 
These  two  pumps  had  capacities  of  about 
250,000  and  400,000  gallons  per  24  hours, 
under  the  pressure  used,  respectively,  and 
were  ones  which  the  Water  Company  had  on 
hand  at  the  time. 

Adaptation  to  Existing  Conditions  in  the  Con 
struction  and  Arrangement  of  These 
Devices. 

In  the  consideration  of  the  construction 
and  arrangement  of  the  devices  which  have 
been  described  in  the  foregoing  pages,  it 
must  be  borne  clearly  in  mind  that  they  were 
designed  to  enable  as  much  practical  'infor 
mation  as  possible  to  be  obtained  in  connec 
tion  with  other  appliances  at  hand,  and  were 
not  intended  to  be  illustrative  of  the  best 
forms  for  adoption  in  practice.  They  were 
arranged  to  yield  data,  with  a  minimum  ex 
penditure  of  time  and  money,  which  would 


show  the  lines  which  it  would  be  most  prac 
ticable  to  follow  on  a  large  scale. 

There  were  many  features  in  the  devices 
which  cannot  be  taken  as  models  of  good 
practice,  although  they  served  their  purpose 
in  this  work.  Thus,  at  the  outset  of  these 
tests,  it  was  known  that  the  settling  basins 
were  all  far  too  small  to  give  the  most  eco 
nomical  and  efficient  results;  the  electrical 
appliances  were  not  well  arranged  to  meet 
the  requirements  of  all  kinds  of  river  water. 
The  question  of  closed  electrolytical  cells  as 
compared  with  open  channels  or  conduits, 
the  thickness  of  metal  plates,  the  water  space 
between  the  plates,  and  the  manner  of  fas 
tening  together  and  insulating  them,  were  all 
open  questions:  and  the  desirability  of  test 
ing  filters  with  different  depths  and  sizes  of 
sand  was  unquestioned.  In  the  discussion 
following  the  results  of  these  tests,  mention 
will  be  made  in  several  instances  of  methods 
for  securing  practicable  results  from  funda 
mental  principles  established  by  these  tests. 

DESCRIPTION  OF  THE  CONDITIONS  AND 
METHODS  OF  OPERATION  OF  THE  DE 
VICES  ARRANGED  BY  THE  WATER  COM 
PANY. 

The  principal  features  concerning  the  gen 
eral  operation  of  these  devices  during  the 
several  periods  from  April  5  to  July  24.  in 
clusive,  1897,  are  as  follows: 

Composition  of  the  River  \\~atcr. —  It  is  dur 
ing  the  period  of  the  year  covered  by  these 
tests  that  the  Ohio  River  water  contains  the 
largest  amount  of  very  minute  clay  particles, 
which,  although  less  in  total  weight  than  the 
heavy  mud  of  the  winter  freshets,  make  the 
water  most  difficult  to  clarify  and  to  purify 
economically.  For  further  reference  to  the 
composition  of  the  river  water  during  the 
spring  and  early  summer,  in  addition  to  com 
ments  beyond,  see  Chapter  I. 

tntcrrnption  of  Tests. — These  investigations 
were  not  continuous,  owing  to  the  fact  that 
the  polarite  system  was  tested  during  this  pe 
riod,  according  to  earlier  arrangements.  This 
caused  the  regular  operations  of  the  devices 
of  the  Water  Company  to  be  suspended  from 
May  10  to  19.  and  from  May  28  to  June  12. 
On  account  of  the  abnormal  clearness  of  the 


342 


WATER   PURIFICATION  AT  LOUISVILLE. 


river  water,  the  operation  of  all  the  devices 
was  not  resumed  after  the  close  of  the  polar- 
ite  tests  until  June  19,  except  the  electrical 
appliances,  which  were  tested  almost  con 
stantly  from  May  30  to  June  30.  Xo  other 
abnormal  interruptions  occurred,  except  from 
May  3  to  5,  when  it  was  impossible  to  obtain 
river  water  which  had  not  settled  for  several 
days  in  the  force  mains. 

Different  Provisions  for  Subsidence. — Three 
settling  basins,  already  described,  were  used 
in  different  ways  (luring-  these  tests,  accord 
ing  to  the  amount  and  character  of  the  sus 
pended  matter  in  the  river  water  and  the  na 
ture  of  the  point  under  investigation.  The 
Jewell  settling  chamber  was  used  without 
exception.  Basins  Nos.  i  and  2  were  both 
used  on  119  different  runs,  as  follows:  April 
1  I  to  May  28,  73  runs:  June  20  to  22,  5  runs; 
June  24  to  July  8,  41  runs.  From  July  14  to 
15.  and  TO  to  19.  basin  Xo.  i  was  used  with 
out  basin  Xo.  2. 

Comparison  of  Different  Coagulants.  —  A 
comparison  was  made  of  the  efficiency  and 
economy  of  hydrate  of  iron,  obtained  electro- 
lytically,  and  from  commercial  sulphates;  and 
of  hydrate  of  aluminum  prepared  electrolytic- 
ally,  and  from  commercial  sulphates.  So  far 
as  practicable  the  several  coagulants  were  ap 
plied  to  practically  the  same  water,  so  as  to 
obtain  comparable  results. 

From  earlier  statements,  it  will  be  recalled 
that  fault}'  insulation  of  electrodes  during 
April  caused  the  electrolytic  results  of  that 
month  to  be  of  uncertain  value.  The  re 
modeled  electrodes  were  tested,  independent 
of  the  filter,  from  May  30  to  June  20. 

Quantity  of  Coagulants.  —  For  obvious 
reasons  the  investigations  were  conducted 
with  the  view  to  determining  the  minimum 
quantity  of  coagulants  which  would  yield  an 
effluent  of  satisfactory,  purity.  In  doing  so 
it  was  necessary  of  course,  at  times,  to  estab 
lish  definitely  that  certain  quantities  were  in 
sufficient.  At  such  times  (usually  short  rnns 
with  the  filter)  the  effluent  was  unsatisfac 
tory;  and,  in  a  measure,  the  results  were 
negative,  although  they  possessed  a  positive 
value. 

Application  of  Coagulants. — In  studying  the 
optimum  method  of  application  of  the  differ 
ent  coagulating  chemicals,  they  were  applied 


so  as  to  give  a  range  of  conditions  with  re 
gard  both  to  the  period  of  coagulation  and 
subsidence,  and  to  the  period  of  coagulation 
prior  to  filtration,  in  the  case  of  waters  of  dif 
ferent  character.  This  range  was  limited  by 
the  capacity  and  facilities  of  the  settling  ba 
sins,  already  described. 

filtration. — The  Jewell  filter  was  operated, 
in  general  terms,  in  a  manner  similar  to  that 
described  in  Chapter  VII,  except  that  there 
was  no  controller  on  the  outlet  pipe,  and  the 
above-mentioned  conditions  of  operation 
called  for  some  changes  at  times  in  the  rate 
of  filtration,  and  frequency  of  washing,  as 
noted  below. 

Rate  of  Filtration. — As  a  rule  the  rate  of  fil 
tration  was  kept  as  nearly  as  possible  at 
250,000  gallons  per  24  hours,  or  94  million 
gallons  per  acre  daily.  This  is  equivalent  to 
23.2  cubic  feet  per  minute,  but  it  was  the  cus 
tom  to  adjust  the  valves  to  give  23.5  cubic 
feet.  Owing  to  the  fact  that  the  electrical 
appliances  were  too  small  to  furnish  sufficient 
electric  current  to  treat  the  water  properly 
when  in  a  very  turbid  condition,  it  w7as  neces 
sary  at  times  to  reduce  the  rate  of  flow  of 
water  through  the  electrolytic  cells,  and,  con 
sequently,  the  rate  of  filtration.  On  sev 
eral  occasions  the  rate  of  filtration  was  re 
duced  for  this  reason  to  about  16  cubic  feet 
per  minute. 

Early  in  these  tests  it  was  found  that  a 
larger  amount  of  coagulating  chemicals  was 
required  just  after  washing  the  filter  than  was 
the  case  during  the  major  portion  of  the  run, 
providing  the  same  rate  was  maintained. 
With  the  view  to  reducing  the  amount  of 
coagulating  chemicals  to  a  point  sufficient  for 
the  latter  portion  of  a  run,  the  rate  of  filtra 
tion  was  reduced  several  times  to  about  one- 
half  the  normal,  for  a  short  period  just  after 
was'hing  the  filter. 

Length  of  Runs. — While  the  regular  custom 
of  allowing  a  run  to  continue  until  the  avail 
able  head  was  exhausted  or  the  quality  of  the 
effluent  failed  prevailed  for  the  most  part, 
there  were  a  number  of  occasions  when  a 
comparison  of  coagulants  required  runs  of 
only  about  1000  cubic  feet  of  effluent.  These 
short  runs  served  the  special  purpose  for 
which  they  were  made,  and,  therefore,  are 
placed  in  the  records,  although  they  were 


INVESTIGATIONS  OF  THE   WATER  COMPANY  FROM  APRIL   TO  JULY,  18H7.    343 


abnormal  so  far  as  length  of  run  is  con 
cerned. 

Washing  tlic  Filter. — Surface  agitation  of 
the  sand  layer  was  employed  whenever  it  was 
practicable.  In  all  cases  of  washing,  it  was 
carried  to  a  point  where  the  wash-water  flow 
ing  to  the  sewer  was  comparatively  clear. 
The  filter  was  always  washed  after  short 
special  runs,  regardless  of  their  length. 

Delays  in  Operation. — In  addition  to  the 
short  delays  incidental  to  such  work,  there 
were  two  sources  of  extended  delays.  The 
first  occurred  several  times  in  April,  when  re 
pairs  of  the  electrodes  were  necessary.  A 
far  greater  cause  for  delay  was  the  change 
of  water  in  all  the  settling  basins  in  service 
which  held  treated  water,  when  there  was  a 
change  either  in  the  rate  or  kind  of  treatment 
to  coagulate  the  water.  It  is  estimated  that 
this  necessary  cause  of  delay  covered  about 
.28  per  cent,  of  the  time  devoted  to  the  actual 
tests. 

Records  of  Operation,  and  Samples  for  An 
alysis. — In  this  respect  the  same  general  plan 
which  was  adopted  in  the  tests  of  1895-96 
was  followed. 

As  a  matter  of  convenience,  and  for  the 
sake  of  clearness,  the  records  of  operation, 
with  summaries  of  analytical  results,  are  pre 
sented  in  the  next  section  by  runs  listed  in 
serial  number,  rather  than  by  days. 

The  general  operations  are  divided  into 
three  periods,  viz: 

Period  No.  I,  which  extended  from  April 
5  to  May  10,  the  beginning  of  the  tests  of  the 
polarite  system. 

Period  No.  2,  which  covered  the  time  oc 
cupied  by  the  changes  made  in  the  polarite 
system. 

Period  No.  3,  which  extended  from  the 
close  of  the  tests  of  the  polarite  system  until 
the  conclusion  of  the  experimental  work. 

In  order  to  facilitate  a  more  thorough  un 
derstanding  of  the  conditions  of  operation, 
and  the  summary  of  results  beyond,  the  fol 
lowing  outline  of  the  important  special  feat 
ures  of  each  period  is  presented. 

Period  No.  I. 

This  period  extended  from  the  beginning 
of  operations  with  these  devices  on  April  5 
to  the  time  when  the  polarite  system  was 


ready  for  operations  on  May  9.  From  April 
5  to  8  operations  were  continuous,  day  and 
night.  On  April  8,  9  and  10,  operations  were 
from  7.00  A.M.  to  6.00  P.M.  on  each  day.  Con 
tinuous  day  and  night  operations  were  begun 
again  on  April  u,  and  continued  through 
out  the  period.  From  April  if>,  2.00  P.M., 
to  April  20,  4.00  P.M.,  and  from  April  24, 
2.44  P.M.,  to  April  26,  6.20  A.M.,  operations 
were  suspended,  to  allow  work  in  repairing 
the  insulation  of  the  electrodes.  The  system 
was  closed  down  on  May  i,  and  from  May  3 
to  5,  inclusive,  attention  was  given  to  labora 
tory  experiments,  as  the  main  pumping  en 
gines  were  not  in  service,  and  it  was  not  pos 
sible  to  obtain  river  water  which  had  not  been 
affected  by  a  varying  period  of  subsidence  in 
the  reservoir  and  pipes.  Operations  were  be 
gun  again  on  May  6,  and  were  continued  till 
5.12  A.M.  on  May  9,  when  the  filter  was  put 
in  shape  for  use  with  the  polarite  system. 

The  river  water  at  the  beginning  of  this 
period  was  about  of  a  normal  character,  the 
suspended  solids  averaging  about  350  parts 
per  million.  A  slight  rise  increased  the  sus 
pended  matter  on  April  9  to  about  840  parts 
per  million.  From  this  date  to  May  i  the 
water  gradually  became  clearer,  the  sus 
pended  solids  on  the  latter  date  averaging 
only  77  parts.  From  May  6  to  9  the  sus 
pended  solids  ranged  from  453  to  301  parts 
per  million. 

During  this  period  66  (Nos.  i  to  66)  runs 
were  made.  From  April  5  to  10,  including 
the  first  14  runs,  operations  were  with  the 
original  Jewell  System,  in  an  unmodified 
form.  Attention  was  devoted  to  a  compari 
son  of  the  efficiency  of  the  hydrates  of  iron 
and  aluminum  obtained  from  persulphate  of 
iron  and  sulphate  of  alumina,  respectively. 
The  first  6  runs  were  without  agitation  of  the 
surface  of  the  filter.  After  this  the  use  of 
surface  agitation  was  made  a  regular  feature 
in  all  runs  continued  to  their  normal  length, 
providing  the  effluent  remained  satisfactory. 

On  April  n  the  full  system  of  devices  ar 
ranged  by  the  Water  Company  was  put  in 
service.  This  system  included  the  three  set 
tling  basins  and  the  Jewell  filter,  together 
with  the  various  devices  for  preparing  and 
applying  the  several  coagulants,  all  of  which 
have  been  described  above. 


344 


WATER    PURIFICATION    AT  LOUISVILLE. 


Coagulants  were  applied  in  equal  amounts 
at  the  inlets  to  basin  No.  2  and  the  Jewell 
settling  chamber,  respectively,  except  on 
runs  Nos.  53,  54,  65  and  66.  On  run  No. 
53  the  entire  chemical  was  applied  at  the  in 
let  to  the  Jewell  settling  chamber,  and  on 
runs  Nos.  54,  65  and  66  at  the  inlet  to  basin 
No.  2. 

Four  differently  prepared  coagulants  were 
used:  Klectrolytically  decomposed  iron,  elec- 
trolytically  decomposed  aluminum,  sulphate 
of  alumina  and  persulphate  of  iron.  Ex 
planation  has  already  been  presented  of  the 
difficulties  met  with  in  the  insulation  of  the 
electrodes,  and  it  will  only  be  noted  here  that 
considerable  uncertainty  is  attached  to  the 
electrolytic  work  during  this  period. 

There  were  two  leading  points  under  con 
sideration  throughout  this  period. 

1.  Comparison  of  the  efficiency  of  the  four 
coagulants  used. 

2.  Determination  of  the  minimum  coagu 
lant  which  could  be  used  with  safety  under 
normal  conditions  of  operation  of  the  system 
used. 

Practically  all  of  the  runs  were  intended  to 
throw  light  on  the  first  point,  and,  in  so  far 
as  possible,  all  coagulants  were  used  on  the 
same  character  of  water.  Of  the  66  runs,  25 
were  made  with  sulphate  of  alumina,  10  with 
persulphate  of  iron,  20  with  electrolytically 
decomposed  aluminum,  and  1 1  with  electro 
lytically  decomposed  iron. 

In  regard  to  the  second  point,  the  rapidly 
changing  character  of  the  river  water,  and  the 
difficulties  experienced  with  the  electrodes, 
interfered  to  a  large  extent  with  this  line  of 
investigation.  Much  information  can  be 
gained,  however,  by  a  comparative  study  of 
consecutive  runs. 

Operations  were  regular  throughout  this 
period,  the  rate  of  250,000  gallons  per  24 
hours  (23.2  cubic  feet  per  minute)  being 
maintained  as  closely  as  possible,  except 
when  the  necessity  of  greater  treatment  than 
the  capacity  of  the  electrolytic  plant  would 
allow  required  a  reduction  in  the  rate. 

Period  No.  2. 

This  period  extended  from  May  19  to  May 
26,  inclusive,  and  included  runs  Nos.  67  to  87. 


Operations  were  continuous  during  the  day 
and  night,  except  for  a  short  delay  from  4.58 
A.M.  to  9.42  P.M.  on  May  21,  to  examine  the 
strainer  system  of  the  Jewell  filter. 

The  river  water  contained  about  280  parts 
per  million  of  fine  suspended  matter  at  the 
beginning  of  the  period.  Absence  of  rains 
caused  the  water  to  become  clearer  during 
the  latter  part  of  the  period,  the  suspended 
matter  decreasing  to  100  parts  per  million. 

Attention  was  devoted  solely  to  the  deter 
mination  of  the  safe  minimum  amount  of  co 
agulant  for  filtration,  in  connection  with  sub 
sidence;  and  for  this  purpose  the  full  system 
of  three  settling  basins  and  the  filter  was  em 
ployed.  Sulphate  of  alumina  alone  was 
used.  It  was  applied  in  all  cases  at  the  inlet 
to  basin  No.  2.  By  the  use  of  these  basins, 
together  with  the  chemical  treatment  at  basin 
No.  2,  the  amount  of  suspended  matter  in  the 
water  at  the  top  of  the  filter  was  usually  kept 
below  TOO  parts  per  million. 

As  it  was  found  that  the  character  and  the 
rate  of  clearing  of  the  first  water  filtered  after 
washing  was  usually  the  controlling  feature 
in  the  consideration  of  the  minimum  amount 
of  coagulant,  several  runs  were  stopped  after 
the  effluent  had  reached  a  fairly  normal  or 
constant  character.  This  procedure  caused 
a  number  of  the  runs  to  be  very  short,  the  ob 
ject  of  several  being  accomplished  with  1000 
cubic  feet  of  effluent,  or  less. 

The  principal  modification  of  the  operation 
was  the  successive  use  of  several  rates,  9,  12, 
1 8,  and  24  cubic  feet  per  minute,  in  order  to 
compare  the  net  amounts  of  coagulants 
needed  for  filtration  at  the  several  rates. 

Period  No.  j. 

This  period  extended  from  June  19  to  July 
24,  when  regular  operations  were  finally  sus 
pended.  In  all  98  runs  were  made,  Nos.  88 
to  185,  inclusive.  Operations  with  the  filter 
were  suspended  011  July  4  and  5,  and  from 
July  10,  at  5.45  P.M.,  to  July  14,  at  8.01  P.M. 
Attention  was  directed  during  the  latter  pe 
riod  to  special  laboratory  tests.  Aside  from 
these  delays,  and  some  minor  ones  incidental 
to  the  methods  of  operation  of  the  system  as 
arranged,  operations  were  continuous  during 
the  day  and  night. 


INVESTIGATIONS  OF  THE   WATER  COMPANY  FROM  APRIL   TO  JULY,  1W7.    345 


Two  minor  rises  of  the  river  occurred  dur 
ing  this  period,  causing  considerable  varia 
tions  in  the  amounts  of  suspended  matter. 
The  range  was  from  66  to  711  parts  per  mil 
lion,  with  an  average  of  320  parts. 

Investigations  were  mainly  along  the  fol 
lowing  lines: 

i.  Comparison  of  efficiencies  of  sulphate  of 
alumina  and  electrolytically  decomposed  iron, 
and  a  determination  of  their  relative  effi 
ciency.  Other  coagulants,  including  persul 
phate  of  iron,  in  which  the  free  acid  had  been 
neutralized  with  caustic  soda,  copperas  (pro- 
tosulphate  of  iron),  alone  and  with  caustic 
soda,  and  electrolytically  decomposed  alumi 
num,  were  also  tried  for  short  periods.  The 
bulk  of  the  work,  however,  was  with  the  first 
two  coagulants,  62  runs  having  been  made 
with  sulphate  of  alumina,  and  26  with  elec 
trolytically  decomposed  iron. 

It  is  to  be  noted  that  the  uncertainties  at 
tached  to  the  early  electrolytic  work  were  re 
moved  during  the  last  of  May  and  early  part 
of  June  by  the  insertion  df  new  insulating  ma 
terials.  On  July  9  electrode  No.  i  was  re 
modeled  to  give  double  the  treatment  which 
was  previously  available. 

2.  Comparison  of  efficiencies  of  various  pe 
riods  of  coagulation  preceding  nitration,  and 
determination  of  minimum  coagulant  allow 
able  with  each.     For  this  purpose  the  place 
of  application  of  the  last  close  of  chemicals 
was  changed  from  time  to  time  to  the  follow 
ing  points:  Inlet  to  basin  No.  i;  inlet  to  basin 
No.  2;    inlet  to  the  Jewell  settling  chamber; 
and  the  outlet  of  the  Jewell  settling  chamber 
(top  of  filter).      For  the  effective  period  of 
coagulation  in  the  several  basins  reference  is 
made  to  the  description  of  these  basins  in  the 
early  part  of  this  chapter. 

3.  Investigations  of  the  rate  of  clearing  of 
the  effluent  following  a  washing  of  the  filter. 
This  point  was  studied  more  or  less  through 
out  the  period  under  different  rates  of  filtra 
tion,  and  with  different  amounts  of  coagulant. 
Several   runs   were   made   specially   for   this 
point,  in  which  the  filter  was  washed  after  the 
first  1000  cubic  feet  or  so  of  water  had  been 
filtered. 

In  order  to  carry  on  these  studies,  use  was 
made  of  basins  Nos.  i  and  2,  and  the  Jewell 
settling  chamber  and  filter,  together  with  the 


devices  necessary  to  prepare  and  apply  the 
various  coagulants.  As  the  river  water 
changed  in  composition  several  times,  it  was 
necessary  to  modify  the  arrangement  from 
time  to  time  during  the  period.  River  water 
was  admitted  directly  to  the  Jewell  settling 
chamber  without  any  preliminary  subsidence 
on  runs  Nos.  88  to  91,  97  to  105,  147  to  156, 
164  to  167,  and  174  to  185,  inclusive.  Basin 
No.  i  only  was  used  on  runs  Nos.  157  to  163, 
and  1 68  to  173,  inclusive.  On  the  other  runs, 
Nos.  92  to  96  and  106  to  146,  inclusive,  ba 
sins  Nos.  i  and  2  were  used. 

The  principal  points  of  significance  in  con 
nection  with  the  various  runs  are  given  in 
serial  order  in  the  following  list.  After  the 
list  is  the  section  containing  the  several  tables 
showing  the  results  of  the  operation  of  these 
devices. 

Notes  on  Special  Features  of  these  Runs. 

Nos.  i  to  7.  Comparison  of  efficiency  of  per 
sulphate  of  iron  and  sulphate  of  alumina, 
using  the  original  Jewell  System,  without 
agitation  of  surface  of  sand  layer. 

Nos.  8  to  14.  Same  as  Nos.  i  to  7,  but  the 
surface  of  the  sand  layer  was  agitated 
whenever  practicable. 

\o.  15.  First  run  with  new  devices,  includ 
ing  three  settling  basins,  filter,  and  de 
vices  for  preparing  and  applying  coagu 
lants.  Iron  plates  of  electrodes  were  new 
and  bright. 

No.  1 8.  The  filter  was  run  dry;  that  is,  the 
sand  layer  was  so  heavily  loaded  with 
suspended  matter  that  surface  agitation 
neither  affected  the  rate  of  filtration  or 
the  character  of  effluent. 

No.  19.  Amount  of  applied  chemicals  was  re 
duced  during  run,  resulting  shortly  in 
failure  in  the  character  of  the  effluent. 

No.  20.  First  run  with  aluminum  electrodes. 
Plates  were  new  and  bright. 

Nos.  20  to  23.  Using  aluminum  electrodes. 
Effluent  failed  suddenly  after  from  2  to 
4  hours'  filtration,  apparently  due  to  ac 
cumulations  of  gas  within  the  sand  layer. 

No.  24.  Flectrode  No.  3  found  touching 
wall  of  the  cell  after  a  short  run.  This 
was  remedied,  and  run  continued. 

No.    26.  Chemical   pump   broke   down,   and 


346 


WATER   PURIFICATION  AT  LOUISVILLE.. 


lack  of  coagulant  caused  an  early  failure 
of  the  effluent. 

No.  27.  Low  voltage  on  cell  No.  3  indicated 
a  leakage  of  electric  current. 

April  1 6.  Repaired  insulations  of  bolts  and 
electrodes. 

No.  32.  Amount  of  treatment  varied  three 
times  during  the  run. 

Nos.  32  to  34.  Resistance  of  electrodes  Nos. 
i  and  3  steadily  falling,  indicating  stead 
ily  increasing  leakage  of  electric  current. 

No.  42.  Electrode  No.  3  found  short  cir 
cuited  after  this  run. 

April  25,  26.  Removed  iron  bolts  from  elec 
trodes  and  put  in  wooden  ones.  Cleaned 
separators. 

No.  44.  First  run  with  repaired  electrodes. 
Plates  had  been  exposed  to  the  air,  and 
were  therefore  heavily  rusted. 

No.  54.  Period  of  service  was  shortened  by 
closing  work  for  the  day. 

No.  70.  This  is  the  only  run  recorded  in 
which  the  hydrate  came  through  the 
sand  layer  into  the  filtered  water  so  as 
to  be  plainly  visible. 

May  30.  Iron  electrodes  reassembled  with 
iron  bolts  and  hard  rubber  insulators, 
and  put  in  service  to  study  the  rate  of 
decomposition  of  the  metal. 

June  3.  Aluminum  electrodes  reassembled 
with  iron  bolts  and  hard  rubber  insu 
lators,  and  put  in  service  to  study  the 
rate  of  decomposition  of  the  metal. 

No.  91.  Several  changes  in  the  rate  of  treat 
ment  and  filtration  were  made  during 
this  run. 

No.  112.  Failed  to  drain  settling  basins  after 
No.  in.  This  run  was  therefore  af 
fected  by  previous  rate  of  treatment. 

No.  127.  Shortened  the  run  to  work  with 
copperas. 

Nos.  133  to  135.  Used  old  aluminum  elec 
trodes,  which  were  very  heavily  coated 
with  oxide.  Direction  of  electric  cur 
rent  was  reversed  several  times. 

Nos.  138,  139.  Application  of  caustic  soda  re 
moved  accumulations  of  organic  matter 
in  the  sand  layer,  and  carried  them  into 
the  effluent. 

No.  147.  Began  to  use  remodeled  electrode 
No.  i. 


No.  149.  Failure  to  supply  coagulant  caused 
an  early  failure  of  the  effluent. 

No.  156.  Period  of  service  was  shortened  by 
closing  work  for  the  day. 

RESULTS   ACCOMPLISHED    BY   THE    DEVICES 

ARRANGED  AND  OPERATED  BY  THE 

WATER  COMPANY. 

The  results  of  chemical  analyses  of  the 
river  water  after  treatment  by  these  methods 
and  devices  are  presented  in  a  series  of  tables, 
in  which  all  of  the  data  obtained  with  the  use 
of  each  coagulant  is  presented  separately. 
With  regard  to  the  collection  and  notation  of 
samples,  methods  of  analysis,  and  significance 
of  results,  reference  is  made  to  Chapter  VIII, 
where  the  corresponding  data  of  1895-96 
were  presented.  For  detailed  information 
concerning  the  composition  of  the  untreated 
river  water,  the  tables  of  analyses  in  Chap 
ter  I  may  be  consulted;  and  the  amounts  of 
suspended  matter,  and  numbers  of  bacteria 
which  on  numerous  occasions  were  deter 
mined  in  samples  collected  as  the  water  left 
the  several  settling  basins,  are  recorded  in  a 
subsequent  portion  of  this  section. 

With  regard  to  features  in  the  chemical 
composition  of  the  effluents,  as  shown  by 
special  analyses,  a  full  account  of  these  mat 
ters  will  be  found  in  the  discussion  of  results, 
which  is  the  closing  portion  of  this  chapter. 
At  this  place  it  may  be  briefly  stated  that  in 
the  case  of  sulphate  of  alumina,  persulphate 
of  iron,  and  protosulphate  of  iron,  the  in 
crease  in  carbonic  acid  and  sulphate  of  lime 
(incrusting  constituents)  in  the  effluent,  was 
proportional  to  the  decrease  in  alkalinity  of 
the  river  water  by  the  respective  treatments. 
With  sulphate  of  alumina,  and  persulphate  of 
iron,  none  of  the  applied  chemicals  in  an  un- 
decomposed  form  appeared  in  the  filtered 
water,  and  there  was  no  diminution  in  the 
oxygen  dissolved  in  the  water.  But  when 
copperas  (protosulphate  of  iron)  was  used, 
the  carbonic  acid  in  the  water  retarded  the 
oxidation  of  the  ferrous  compounds  by  the 
dissolved  oxygen,  so  that  when  this  chemical 
alone  was  used,  some  of  the  iron  passed  into 
the  effluent.  The  use  of  caustic  soda  in  con 
nection  with  copperas  changed  the  carbonic 


INVESTIGATIONS  OF  THE  WATER  COMPANY  FROM  APRIL  TO  JULY,  18H7.   347 


acid  to  carbonate  of  soda,  and,  under  these 
conditions,  copperas  could  be  satisfactorily 
applied  as  a  coagulant,  provided  the  amount 
applied  was  not  in  excess  of  that  capable  of 
oxidation  by  the  constituents  of  the  water. 
It  caused  a  reduction  for  each  grain  per  gal 
lon  of  about  0.5  part  of  dissolved  oxygen, 
which  was  required  in  order  to  convert  the 
iron  into  a  completely  insoluble  form.  In 
passing,  it  may  be  noted,  that  the  application 
of  caustic  soda  caused  a  marked  removal  of 
the  organic  matter  accumulated  on  the  sand 
grains  of  the  filter,  as  shown  by  the  analyses. 
In  those  cases  where  common  alum  crystals 
were  used  as  a  coagulant  the  normal  free  am 
monia  in  the  effluents  is  estimated  because 
the  coagulant  contained  some  ammonia. 

Concerning  the  special  chemical  features  of 
the  effluent  obtained  with  electrolytic  treat 
ment,  there  were  no  additional  carbonic  acid, 
incrusting  constituents,  or  dissolved  metal  in 
the  water  as  it  left  the  filter  under  ordinary 
conditions.  With  aluminum  electrodes  this 
was  true  under  all  conditions;  but  with  iron 
electrodes  the  decomposed  iron  had  to  be  oxi 
dized  by  dissolved  oxygen,  in  order  to  convert 
it  into  a  completely  insoluble  form.  As  in 
the  case  of  copperas,  therefore,  the  electro 
lytic  iron  treatment  could  not  be  safely  em 
ployed  beyond  a  certain  amount,  which  was 


limited  by  the  oxygen  dissolved  in  the  water. 
Otherwise,  dissolved  iron  would  pass  into 'the 
filtered  water. 

Microscopical  analyses  were  not  made 
regularly,  but  from  occasional  examinations 
of  the  effluents,  it  may  be  stated  that,  as  was 
the  case  during  1895-96,  the  effluents  were 
practically  free  from  microscopical  organ 
isms. 

The  results  of  the  bacterial  analyses  of  the 
effluent  with  each  coagulant  are  presented  in 
the  set  of  tables  following  the  chemical  re 
sults,  and  are  given  in  the  same  form  as  was 
used  and  explained  in  Chapter  VIII.  There 
are  no  special  features  worthy  of  comment 
in  this  connection,  except  perhaps  to  point 
out  the  fact  that,  repeatedly,  turbid  effluents 
were  found  to  give  a  fairly  satisfactory  bac 
terial  efficiency.  In  no  case,  however,  was 
an  admissible  bacterial  efficiency  obtained 
when  the  coagulation  of  the  water  passing 
on  to  the  sand  layer  was  lacking  to  a  marked 
degree. 

These  analytical  results  are  summarized  by 
runs,  together  with  a  record  of  the  kind, 
method  of  application,  and  quantity  of  co 
agulating  teatment,  and  of  quantities  of  water 
treated,  with  corresponding  periods  of  time, 
at  the  close  of  this  section.  A  full  explana 
tion  of  this  summary  precedes  it. 


WATER   PURIF1CTA1ON  AT  LOUISVILLE. 


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W 'A  TER   PURIFICATION  AT  LOUISVILLE. 


RESULTS   OF    BACTERIAL   ANALYSES   OF   THE    EFFLUENT   OF    THE   JEWELL    FILTER    WITH 

SULPHATE   OF   ALUMINA. 


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"      16 

2.3O  A.M. 

28 

23-5 

95 

4.0 

2h.  45m. 

3755 

471 

5447 

"      16 

3.00      " 

28 

23-5 

95 

3-1 

ih.  38m. 

2329 

269 

5448 

"      16 

5-00      " 

30 

23-5 

95 

3-i 

oh.  38111.      i  031 

68 

5449 

"      16 

6.00     " 

30 

23.0 

93 

3-0 

ih.  38111. 

2  401 

49 

5499 

"       22 

9-3°    " 

36 

23.5 

95 

3-o 

ih.  33m. 

2  099 

61 

5500 

"       22 

10.30    " 

36 

23-5 

95 

3-4 

2h.  33111. 

3499 

i  450 

5501 

"       22 

11.30    " 

36 

23-5 

95 

3.8 

3h.  33111. 

4959 

37 

5502 

"       22 

I2.3O   P.M. 

36 

23  5 

95 

4.0 

4h.  33m.     6349 

68 

55°3 

"       22 

I.30      " 

36 

23-5 

95 

4-3 

5h.  33m.     7659 

55 

5504 

"       22 

2.30      " 

36 

23-5 

95 

4.8 

6h.  33m.     S  859 

165 

5509 

"       22 

3-30      " 

36 

23.0 

93 

5-0 

7h.  33111.    10269 

335 

5533 

"       24 

g.OO  A.M. 

43 

23-5 

95 

3-7 

2h.  40m.      3  521 

24 

5534 

'       24 

10.00      " 

43 

23-5 

95 

3-9 

3h.  4om.     4  881 

26 

5535 

"       24 

I  I.OO      " 

43 

23.0 

93 

4-2 

4h.  40111.     6  221 

26 

5536 

'       24 

12.  OO     M. 

43 

23-5 

95 

4-9 

5h.  4om.     7  611 

21 

5537 

"      24 

I.OO   P.M. 

43 

23-5 

95 

5-0 

6h.  4om.i    9011 

59 

INVESTIGATIONS  OF  THE  WATER  COMPANY  FROM  APRIL   TO  JULY,  IS'.il.  351 


RESULTS    OF    BACTERIAL    ANALYSES— WITH    SULPHATE    OF  -ALUMINA.  —  Continued. 


1 

R-il 

.. 

I  S 

1 

Collected. 

Filtration. 

t 

0 

IS 

1 

Number 

s. 

JsL 

•d 

Period  of 
Service  Since 

at-- 

u  u. 

z 

of 
Run. 

I,; 

'3  t;  1 

X 

Last 

SsarTd 

m 

«  S 

Remarks. 

Date. 

Hour. 

o  c 

c<'i 

"3 

Minutes. 

u  tr2 

aj  C 

•E 

la 

=  g.  » 

0 

«J  «  3 

=  JO 

|(5 

« 

u 

s 

>s 

u. 

03 

1897 

5538 

April  24 

2.30  P.M. 

43 

23-5   95 

6.0 

8h.  iom. 

II  OOI 

242  Closed  outlet  at  2-44  P.M. 

5589 

"   29 

4.00  A.M. 

50 

23.0   93 

oh.  3gm.    764    43 

5591 

"  29 

5.00   " 

50 

23.0   93  

ih.  39m.   2  024     44 

5592     '   29 

6.00  " 

50 

23-0   93   3.0 

2h.  39111.  3424'    23 

5593    "   29 

9.00 

50 

23-5   95   4-5   5h.  sgm. 

8  664    24 

5595    "  29 

10.00   " 

50 

23-5   95   5-2   6h.  sgm. 

9  044     22 

5596    '  29 

II.OO   " 

50 

23-5   95 

6.2   7h.  3gm.  10454    45 

5600   "  29 

12.  OO  M. 

50 

23-5   95 

7-5 

8h.  3gm.  11907    107  Agitated  surface  of  sand  layer  at 

5601   "  29 

1.  00  I'.M. 

50 

23-5   95 

6.0 

gh.  37m.  13397    H7 

12.24  !'-M- 

5602!   "  29 

2.OO   " 

50 

23.0   93 

6.6 

toh.  37m.  i  14747    173 

5603 

'  29 

3.OO   " 

50 

23-5 

95 

7-7 

iih.  35111. 

16  120    510  Closed  outlet  at  3.08  P.M. 

5762 

May  7 

9.00   " 

59 

23-5 

95 

2-7 

oh.  48m. 

I  158 

46 

5763 

7 

10.00  " 

59 

23-5 

95 

3.0   in.  48m. 

2588 

M9 

7 

II.OO   " 

59 

23-5 

95 

3.2   2h.  48171. 

3968 

71 

5768 

7 

12.00   " 

59 

23-5 

95 

3.6   3h.  4Sm. 

5318 

123 

5773 

8 

4.00  A.M. 

60 

23-5 

95 

2.6   oh.  57m. 

I  369 

.89 

5774 

8 

5.00  " 

60     23  .  5 

95 

3.0   ih.  57m. 

2  769 

58 

578o 

"   8 

9.30  " 

61 

23-5   95 

3.5   2h.  3om. 

3510    76 

578i 
5782 

8 
8 

IO.OO 
II.OO 

6  1 
61 

23-5 
23-5 

95 
95 

3-8 
3-9 

3h.  oom. 
4h.  oom. 

4220   311 
5660   116  Closed  outlet  at  11.04  A.M. 

5783 

8 

I2.OO  M. 

62 

23-5 

95 

3-0 

oh.  33m.    747    18 

5784 

•'   8 

1.  00  P.M. 

62 

23-5 

95   Z.6 

ih.  33111.  2  197    89 

5785 
5786 

8 
8 

2.OO   " 
2.3O 

62 
62 

23-5 
23.0 

95 
93 

3-4 

3-7 

2h.  33m. 
3h.  0301. 

3577   "o 
4  167    129 

Closed  outlet  at  2.35  P.M. 

5787 

8 

3-05   " 

63 

23-5 

95 

oh.  05m. 

119    122 

5788 

"   8 

3.08   " 

63 

23-5 

95 

oh.  iom. 

239    37 

5789 

8 

3-13   " 

63 

23-5 

95 

oh.  ism. 

359    57 

5794 

8 

4-3"  " 

63 

23.0 

93 

2.6 

ih.  32m. 

2  089 

.22 

5795 

8 

5-3"  " 

63 

23-5 

95 

3-0 

2h.  32m. 

3  54<» 

105 

b796 

"   8 

8.(X>  " 

64 

23.5 

95 

2.8 

oh.  2Sm. 

f'7  1 

191 

5797 

8 

9.00 

64 

23-5 

95 

3-4 

ih.  28m. 

2  051 

142 

5799 

8 

II.OO   " 

65 

23-5 

95 

2  5 

oh.  27m. 

735 

189 

5800 

"   8 

12.  OO   " 

65 

23-5 

95 

2-7 

ih.  27m. 

2055 

74 

5801 

9 

1.  00  A.M. 

65 

23-5 

95 

2-9 

2h.  27m. 

3445 

142 

5802 

9 

1.30   " 

65 

23.?   95 

3.0 

2h.  57m. 

4  I°5 

92 

Closed  outlet  at  1.43  A.M. 

5803 

9 

3-3"  " 

66 

23-5 

95 

2-5 

oh.  oim. 

23    4i 

5804 

9 

4-3"  " 

66 

23-5 

95 

2.7 

ih.  oim. 

I  433    45 

5964 

'  19 

II.oo  I'.M. 

67    23.5 

95 

2.1 

oh.  56m. 

t246 

272 

5968 

'  19 

12.  OO   " 

f'7    23.5 

95 

2.8 

ih.  56m 

2  606 

196 

5969 

"  20 

I.(X)  A.M. 

f>7    23.5 

95 

2-9 

2h.  56m. 

3966 

490 

5971 

"  20 

3-OO 

68 

12.  0 

48 

0.8 

oh.  33m. 

381 

274 

5972 

"   20 

4-00   " 

68 

12.0 

48 

0.9 

ih.  33m. 

I  181 

M4 

5973 

"   20 

5.00   " 

68 

12.0 

48 

1.0 

2h.  33m. 

I  821 

139 

5974 

2O 

6.00  " 

68 

12.0 

48 

I  .2 

3".  33m- 

2  621 

I  080 

5976 

"   2O 

9.00  " 

68 

12.  O 

48 

i.S 

6h.  33m. 

4891 

3900 

5977 

"   20 

II.OO   " 

68 

12.  O 

48 

1.9 

8h.  33m. 

6381 

244 

5978 

"   20 

1.  00  P.M. 

68 

12.0 

48 

2.2 

loh.  33m. 

7841 

308 

5980 

"   20 

3.OO 

68 

12.0 

48 

2.8 

I2h.  33m. 

9381 

395 

"   20 

5.30   " 

68 

12.  0 

48 

3-1 

I4h.  53tn. 

II  26l 

165 

5985 

,,   20 

8.00  " 

68 

12.0 

48 

4.1 

i?h.  33m. 

13  221 

230 

,,   20 

9.00  " 

68 

12.0 

48 

4-4 

l8h.  33m. 

I395I 

343 

jggE 

,,   20 

II.OO   " 

69 

23-5 

95 

2.5 

oh.  48m. 

I  080 

401 

5989 

.,   20 

12.  00   " 

69 

23.5 

95 

2.6 

ih.  48m. 

2460 

4500 

5990 

"   21 

1.  00  A.M. 

69 

23.5 

95 

2.8 

2h.  48m. 

3810 

307 

5991 

"   21 

2.OO   " 

69 

23-5 

95 

3-0 

3(1.  48m. 

5  180 

635 

5993 

"   21 

3-oo  " 

69 

23-5 

95 

3-2 

4h.  48m. 

6680 

I  760 

5994 

"   21 

4.(X>  " 

69 

23-5 

95 

3-5 

5h.  48m. 

7950 

215 

5995 

"   21 

4-3"  " 

69 

23-5 

95 

3-7 

6h.  l8m. 

863c 

375 

Closed  outlet  at  4.41  A.M. 

5997 

"   21 

I0.3'J  P.M. 

7° 

12.0 

48 

I.O 

oh.  3801. 

480 

417 

5998 

"   21 

12.  (X)   " 

70 

12.  0 

P 

1.0 

2h.  o8m. 

I  480 

397 

5999 

"   22 

I.OO  A.M. 

7" 

12.  0 

r 

1.  1 

3h.  o8m. 

t  400 

259 

6000 

"   22 

2.OO   " 

70 

12.0 

48 

I  .2 

4h.  o8m. 

3  u" 

460 

6002 

"   22 

3.OO   " 

70 

12.0 

48 

1-5 

5h.  o8m. 

3860 

257 

6006 

"   22 

5.OO   " 

70 

12.  0 

r 

1.8 

7h.  o8m. 

5  380 

423 

352 


WATER   PURIFICATION  AT  LOUISVILLE. 


RESULTS    OF    BACTERIAL   ANALYSES— WITH    SULPHATE   OF   ALUMINA.  —  Conti 


Rate  of 

{J 

% 

Collected. 

Filtration. 

£ 

•^ 

-H 

|~u 

Period  of        ^  a 

.3 

OJ 

Number       g. 

§  a 

T3 

S'.  rviceSince     i--  j 

u 

a 
P 
x 

Run.          a  v 

t  :j 

-3  £  j» 

C  0  3 
^  <  0 

I 

Washing.      &"£ 
Hours  and       -a=  o 

S.U 

Remarks. 

Date. 

Hour. 

0  UI 

° 

Minutes. 

£  3.0 

<D  - 

•~ 

II 

^  a? 

1 

•=33 

^U 

I/I 

O 

S 

- 

it 

n 

1897 

6008 

May  22 

9.00  A.M. 

70 

I2.O 

4S 

3-2 

nh.  o8m.      7  943 

241 

6009 

"      22 

I2.OO  M. 

70 

12.0 

48 

5-5 

I4h.  oSm.      I  015 

380 

6011 

"       22 

3.00  P.M. 

70 

12.0        .(S 

8.2 

I7h.  oSm.    12  303 

362 

6012 

"       22 

5-30    " 

70 

12.0         48 

il.  7 

igh.  38111.    14203 

546 

Agitated  surface  of  sand  layer  at 

6013 

"       22 

5-45      '                    70 

12.0        48 

3-o 

igh.  4gm.    14403 

635 

5.30  P.M. 

6014 

"       22 

7.00    "               70 

12.0        48 

3-2 

2ih.  0401.    15  543 

472 

6016 

"       22 

9.00     "                 70 

12.0        48 

3-9 

23!!.  04m.    17  013 

498 

6020 

"       22 

11.00       "                         70 

12.0        48 

4.0 

25h.  04111.    18  513 

578 

6021 

"       23 

I.OO  A.M.                      7O 

12.0        48 

4-5 

27h.  O4m.   20013 

497 

6023 

"       23 

3.00     "                 70 

12.0        48 

5-1 

2i)h.  04tn.   21  543 

262 

6024 

"       23 

6.00     "                   70 

12.0        48* 

6.0 

32h.  04111.   23643 

Sio 

6025 

•'       23 

7.00     "                 70 

12.0        48 

6.1 

33h.  04111.   24433 

750 

f)027 

'      23 

9.00     "                   70 

12.0        48 

6   5 

35h.  04m.   25643 

995 

6028 

'     23 

12.30    P.M.                      70 

12.  O        48 

S.i     39h.  04111.   28  223 

I  270 

6030 

'    23 

3.00    "               70 

12.0        48 

9.  i    41  h.  04111.   30093 

610 

603  1 

'    23 

4.30    "               70 

12.0        48 

10.  1    42h    34111.   31  203 

I  OOO 

Agitated  surface  of  sand  layer  at 

6032 

"     23 

6.30    "              71 

23-5        95 

2.0,     oh.  3om.        720 

2  290 

4.30  P.M.  Closed  outlet  at  4.45P.M. 

6033      "    23 

7.00    "              71 

23.5      95 

2.2      ih.  oom.      I  410 

I  890 

Closed  outlet  at  7.11  P.M. 

6034      '  '    23 

9.00     "                   72 

23-5      95 

2.1,     oh.  43111.        935 

I  020 

6036      "    23 

10.00     "                   72 

23-5      95 

2.3      ih.  43111.     2  275 

26l 

6037      "    24 

12.30  A.M.                      72 

23-5      95 

2.8      4h.  1301.      5645 

242 

6038 

"    24 

2.01)       "                         72 

23-5      95 

3.4      sh.  43m-      7635 

4lS 

6040 

'    24 

3.00     "                   72          23.5      95 

3.6      6h.  43111. 

9005 

725 

6041 

'     24 

4.00     "                   72 

23-5      95 

3.9      7h.  43.11. 

10  565 

460 

6042 

'    24 

6.00     " 

72 

23-5      95 

4.8:     gh.  43m. 

13075 

185 

6044 

'    24 

9.00    " 

72 

23-5      95 

6.  Sj   I2h.  43m. 

17  135 

235 

Closed  outlet  at     9.10  A.M. 

48 

...  i  

I  26o 

6047 

24 

'    24 

9-3°  r.M. 

10.00        " 

I  J 

73 

2.0 

48 

I  .  i 

ih.  lorn. 

480 

2  250 

"   10.24  t'-M- 

6048 

"    25 

I.OO  A.M. 

74 

2.0 

48      i.o 

oh.  32111. 

362 

4  5°o 

6049 

"     25 

2.00       " 

74 

2.0 

48 

1  .0 

ih.  32111. 

I  062 

2  95" 

Closed  outlet  at  2.18  A.M. 

6051 

"     25 

5.oo     " 

75 

2.O 

48 

I.O 

oh.  52m. 

479 

54" 

6056 

"    25 

6.00 

75 

2.0       48        I.I 

ih.  52m. 

i  219 

235 

6058 

"    25 

9.00     " 

75 

2.0        48         I.f) 

4h.  52m. 

3  559 

260 

0059 

'    25 

II.  oo     "                   75 

2.0        48    ^    1.8 

6h.  5201. 

5  159 

125 

6060 

"    25 

I.OO   P.M. 

75 

2.0        48        2.0 

8h.  52m. 

6649 

263 

6062 

"    25 

3.00     " 

75 

2.0        48        2.8 

loh.  5201. 

8  IK) 

375 

6063 

"    25 

5.3°    " 

75 

2.0      48      3-3 

I3h.  22m. 

9  949 

342 

6064 

"     25 

7.30    " 

75 

12.0        48        4.2 

I5h.  22m. 

II  449 

495 

Closed  outlet  at  7.30  P.M. 

6066 

"    25 

0.  10       " 

76 

12.  O 

48    .... 

oh.  ism. 

174 

595 

6067 

"     25 

0.15      " 

76 

12.0 

48    .... 

oh.  2om. 

234 

54" 

6068 

"    25 

o.  20     " 

76 

12.  O 

48    .... 

oh.  25m. 

295 

520 

6069 

•'    25 

0.25      ' 

76 

12.  O 

48    .... 

oh.  3om. 

354 

391 

6070 

"    25 

2.00       " 

77 

9.0 

34 

oh.  2901. 

284 

420 

6071 

"    26 

2.OO  A.M. 

78 

23-5 

95      2.1 

oh.  45m. 

996 

223 

6072,      "     26 

2.36       " 

79 

23-5 

95 

2.8 

oh.  05111. 

88 

419 

6073 

11    26 

2.41        " 

79 

23-5 

95 

oh.  lorn. 

208 

435 

6074 

"    26 

2.46       " 

79 

23-5 

95     •••• 

oh.  15111. 

308 

352 

6075 

"    26 

2.51       " 

79 

23-5 

95 

30 

oh.  2om. 

418 

315 

6077 

"    26 

3.15       ' 

79 

23.5 

95 

oh.  44111. 

95S 

109 

Closed  outlet  at  3.25  A.M. 

6078 

"    26 

5-45       ' 

So 

23-5 

95 

oh.  iSm. 

393 

497 

6079 

"    26 

6.00     " 

80 

23-5 

95 

2.1 

oh.  33m. 

713 

STO 

6081 

"    26 

9.00     " 

8 

23-5 

95 

2.2 

oh.  3om. 

697 

301 

6082 

"    26 

10.00        " 

8 

23.5 

95 

2.6 

Ih.  3Om. 

2  067 

35(> 

6083 

"       2& 

I  I.OO       " 

8 

23.5 

95 

2.8 

2h.  3om. 

3477 

339 

6084 

"    26 

12.00  M. 

S 

23-5 

95 

3-o 

3h.  3«m. 

4847 

268 

6085 

"    26 

2.00  P.M. 

8 

23.0 

93      3-5 

5h.  30m. 

7597 

229 

6087 

"    26 

3-30    " 

8 

23.0 

93 

3-8 

7h.  oom. 

9657 

235 

6088 

"    26 

5-3°     " 

8 

23-5 

95 

4.8 

9h.  oom.]  12  497 

319 

6089 

"    26 

7.00     " 

8 

23.5 

95 

5-4 

i  oh.  3om. 

M397 

216 

6090 

6095 

"    26 

"    26 

8.30     " 
10.52     " 

8 
8 

23-5 
23.0 

95 
93 

6.4 

I2h.  oom. 
I4h.  22m. 

16517 
19597 

304 

338 

Agitated  surface  of  sand  layer  at 

6096 

"    26 

11.05      " 

8 

23.5 

95 

I4h.  3im. 

19747 

432 

10.53  i'-M. 

6097 

"    26 

II.  10       " 

8 

23-5 

95 

5.0 

I4h.  36m. 

19847 

263 

6098 

"     27 

I.OO  A.M. 

8 

23-5 

95 

6.0 

i6h.  26m. 

22327 

311 

INVESTIGATIONS  OF  THE   WATKR  COMPANY  FROM  APRIL   TO  JULY,   1807. 


RESULTS    OF    BACTERIAL    AN ALYSES— WITH    SULPHATE    OF    ALUMINA.— Continued. 


Rat 

eof 

*j 

- 

C 

ollccted. 

Filtr. 

fc, 

Ji 

2 

^ 

u 

e  4j 

Period  of 

u  ^ 

T3 

£ 

£ 

Number 

8. 

=  a  . 

i 

Last 

3-=  | 

<i$ 

Remarks 

3 

X 

Hate. 

Hour. 

Run. 

?i 

5  Ss' 

-•«  o 
5  ..E 

£ 

Washing. 
Hours  and 
Minutes. 

ill 

II 

PC 

•^s 

^  a  cT 

$ 

^JO 

su 

tn 

u 

s 

j 

b. 

o 

1897 

6100 

May  27 

3.00  A.M. 

Si 

23.5 

95 

7-o 

i8h.  26m. 

25057 

382 

6101 

"     27 

4.05      " 

82 

23-5 

95 

oh.  o7m. 

145 

522 

6l(j2 

"     27 

4.10     " 

82 

23-5 

95 

Oh.    I2IT1. 

245 

575 

6103 

"     27 

4.22      " 

82 

23-5 

95 

oh.  24m. 

545 

499 

6104 

"     27 

4-43      ' 

82 

23-5 

95 

oh.  45m. 

I  045 

370 

Closed  outlet  at  4.44  A.M. 

6105 

"     27 

5-23      ' 

83 

12.0 

48 

oh.  lorn. 

128 

411 

6106 

'     27 

5-34      " 

83 

12.0 

48 

oh.  21  m. 

235 

298 

6107 

"     27 

5-54      ' 

S3 

12." 

48 

oh.  4im. 

498 

453 

6109 

'     27 

9-05      ' 

84 

12.0 

48 

oh.  lorn. 

150 

590 

6110 

"     27 

9.18      ' 

84 

12.0 

48 

oh.  23m. 

2gS 

382 

6jn 

"     27 

9-35     " 

84 

12.  0 

48 

oh.  4om. 

498 

272 

6112 

'     27 

10.16     " 

84 

12.0 

48 

ih.  2im. 

998 

197 

1113 

"     27 

10.24     " 

84 

23-5 

95 

ih.  29111. 

i  168 

193 

6114 

"     27 

II.  OO        " 

84 

23.5 

95 

2h.  05111. 

2018 

227 

6115 

"     27 

12.  OO  M. 

84 

23.5 

95 

3h.  osm. 

3388 

215 

6116 

"     27 

1.  00  P.M. 

84 

23-5 

95 

4h.  0501. 

4788 

161 

6117 

"     27 

2.00       " 

84 

23.5 

95 

5h.  osm. 

6188 

305 

6119 

'     27 

3-00       " 

84 

23-5 

95 

5-') 

6h.  osm. 

7558 

167 

6120 

"     27 

4.00     " 

84 

12.5 

50 

3-7 

7h.  osm. 

8368 

162 

6121 

'     27 

5.00    •' 

84 

12.0 

48 

4-3 

8h  .  osm. 

9098 

'95 

6122 

'     27 

6.  oo     " 

84 

12.0 

48 

5-" 

gh.  05111. 

9838 

164 

Closed  outlet  at  6.00  P.M. 

6123 

•     27 

8.14     " 

85 

12.0 

48 

Oh.    I2IT1. 

150 

529 

6124 

'     27 

8.22       " 

85 

12.  O 

48 

oh.  2om. 

250 

342 

6125 

"     27 

8-43       " 

85 

12.0 

48 

oh.  4im. 

530 

302 

6126 

'     27 

9-'5       " 

85 

12.  O 

48 

Ih.  I3m. 

950 

233 

6127 

'    27 

9-25       ' 

85 

23-5 

95 

ih.  23m. 

i  150 

269 

6128 

'    27 

9.30       " 

85 

23.5 

95 

ih.  28m. 

i  250 

371 

6129 

"     27 

9-35       ' 

85 

23.5 

95 

Ih.  33m. 

i  380 

337 

Closed  outlet  at    9.45  P.M. 

6131 

"       27 

0.17       ' 

86 

23.5 

95 

oh.  o6m. 

138 

480 

6132 

"    27 

O.23       " 

86 

23.5 

95 

oh.  I2m. 

258 

295 

6133 

"     27 

0.32       " 

86 

23-5 

95 

oh.  2im. 

498 

3" 

"           "       "  10.46  P.M. 

6134 

"    28 

2.43  A.M. 

87 

23.5 

95 

oh.  o8m. 

145 

228 

6135 

••    28 

2.4S       " 

87 

23.5 

95 

oh.  1301. 

245 

263 

6136 

"    28 

2.58       " 

87 

23-5 

95 

oh.  23m. 

495 

H7 

6138 

••    28 

3.00      " 

87 

23-5 

95 

2.5 

2h.  25m. 

3225 

89 

6142 

"      28 

4-30      " 

87 

23.5 

95 

2.8 

3h.  55m. 

5305 

231 

6143 

"    28 

6.  c»     " 

87 

23-5 

95 

3-5 

5h.  2501. 

7335 

104 

6144 

"    28 

8.00     " 

87 

23.5 

95 

4.0 

7h.  25m. 

0065 

510 

6146 

"    28 

9.00     " 

87 

23.0 

93 

4-7 

8h.  25m. 

1435 

188 

6147 

"    28 

10.00       " 

87 

23.0 

93 

5-4 

gh.  25m. 

2805 

222 

6148 

•'   28 

II.  OO       " 

87 

23-5 

95 

6.4 

loh.  25m. 

4185 

'97 

6149 

"    28 

11.30     " 

87 

23-5 

95 

6.9 

loh.  55m. 

4885 

254 

Closed  outlet  at  11.34  A.M. 

6520 

June  20 

4.53  P.M. 

92 

23.0 

93 

oh.  osm. 

114 

396 

6521 

"     20 

4.58  " 

92 

20.0 

81 

oh.  lorn. 

211 

4OO 

6522 

"       20 

5.03    " 

92 

24.0 

97 

oh.  ism. 

309 

388 

6523 

"      20 

5.13    " 

92 

23-5 

95 

oh.  25m. 

564 

295 

* 

6524 

"      2O 

6.  oo     " 

92 

23.5 

95 

3-0 

ih.  I2m. 

I  574 

357 

6525 

"      2O 

7.00     " 

92 

23-5 

95 

3-8 

2h.  I2m. 

2904 

'57 

6526 

"       20 

S.oo     " 

92 

23-5 

95 

4-7 

3h.  I2m. 

4254 

247 

Closed  outlet  at  S.io  P.M. 

6527 

"       20 

1.45     " 

93 

23-5 

95 

oh.  osm. 

in 

198 

6528 

"       20 

1.53     " 

93 

23.5 

95 

oh.  I3m. 

3" 

153 

6529 

"       20 

2.OO       " 

93 

23-5 

95 

2.2 

oh.  2om. 

501 

130 

6530 

"       21 

2.10  A.M. 

93 

23.5 

95 

oh.  3om. 

701 

184 

6532 

"       21 

2.30       " 

93 

23-5 

95 

2-5 

oh.  sotn. 

I  161 

117 

6533 

"      21 

1.30       " 

93 

23--) 

95 

3-o 

ih.  som. 

i  541 

138 

6534 

"       21 

2.30       " 

93 

23.5 

95 

3-7 

2h.  som. 

3861 

345 

6536 

"      21 

3.30       " 

93 

23-5 

95 

4-7 

3h.  som. 

5  231 

945 

Closed  outlet  at  3.45  A.M. 

'•=  >7 

"      21 

5.2"       " 

94 

23-5 

95 

oh.  07m. 

184 

"5 

'  •  -  i  • 

"       21 

5.30   " 

94 

23.5 

95 

2-3 

oh.  I7m. 

434 

138 

6539 

"      21 

6.0"      " 

94 

23-5 

95 

2-5 

oh.  47m. 

I  214 

76 

(,=  |i 

21 

9.00     " 

94 

22.0 

3-0 

3h.  47m. 

5  304 

94 

6542 

"      21 

IO.OO        " 

94 

L'd.o 

105 

4.0 

4h.  47m. 

6654 

155 

6543 

"      21 

11.00       " 

94 

23-5 

95 

4.0 

5h.  47m. 

8054 

425 

6544 

"       21 

12.  OO       " 

94 

23.5 

95 

4-5 

6h.  47m. 

9444 

395 

354 


WATER  PURIFICATION  AT  LOUISVILLE. 


RESULTS    OF    BACTERIAL    ANALYSES— WITH    SULPHATE    OF    ALUMINA.— Continued. 


Rate  <>i 

~ 

0 

Collected. 

Filtration. 

a 
b 

c 

IS 

J3 

Number 

a 

o  a 

•a 

Period  of 
ServiceSince 

o3  ^ 

u  u. 

G 

jjj 

is': 

X 

Last 
Washing. 

£j££ 

ks 

Remarks. 

if 

Date. 

Hour. 

^  3 

lul 

Hours  and 
Minutes. 

|s| 

il 

£ 

U 

=  a  ? 

2 

b 

cc 

1897 

6545 

June  21 

I.OO    P.M. 

94 

23-5 

95 

4.8 

7h.  47m. 

10854 

315 

6546 

"       21 

2.00       " 

94 

23-5 

95 

5-1 

8h.  47m. 

12254 

6548 

"       21 

3-oo     " 

94 

23-5 

95 

5-7 

gh.  47m. 

13644 

287 

6549 

"       21 

4.30     " 

94 

23-5 

95 

6.0 

Iih.  I7m. 

15  754 

6550 

"       21 

5.00     "                   94 

23-5 

95 

6-3 

nh.  47m. 

16424 

328 

6551 

"       21 

8.03     "                   95 

23-5 

95 

2.2 

oh.  O5m. 

126 

162 

6552 

"       21 

8.  10     "                   95 

23-5 

95 

oh.  I2m. 

266 

156 

6554 

"       21 

8-30     "                   95 

23-5 

95 

2.8 

oh.  32m. 

736 

126 

6555 

"       21 

8.40     "                   95 

23-5 

95 

oh.  42m. 

986 

105 

Closed  outlet  at  8.41  P.M. 

6556 

"       22 

12.52  A.M.                 96 

23-5 

95 

oh.  osm. 

103 

198 

6557 

"       22 

I.OO       "                          96 

23-5 

95 

2-5 

oh.  I3m. 

343 

218 

6558 

"       22 

I.  10       "                          96 

23.5 

95 

oh.  23m. 

5°3 

253 

6559 

"       22 

1.20      "                        96 

23-5 

95 

oh.  33m. 

733 

290 

6560 

"       22 

1.30    "               96 

23-5 

95 

2.6 

oh.  43m. 

I  023 

3M 

Closed  outlet  at  1.34  A.M. 

6562 

"       22 

4-45     '                     97 

23-5 

95 

oh.  05m. 

95 

39° 

6563 

"       22 

4.53     '                     97 

23-5 

95 

oh.  I3m. 

275 

495 

6564 

"       22 

5.00     "                   97 

23-5 

95 

2.5 

oh.  2om. 

475 

415 

6565 

"       22 

5-3°     "                    97 

23-5 

95 

2.5 

oh.  som. 

I  165 

157 

6566 

"       22 

6.00     "                   97 

23-5 

95 

2.6 

ih.  2om. 

i  865 

305 

Closed  outlet  at  6.11  A.M. 

6568 

"       22 

9.  10     "                   98 

24.0 

97 

oh.  osm. 

140 

146 

6569 

"       22 

9.15     "                   98 

23-5 

95 

oh.  lorn. 

260 

Si 

6570 

"       22 

10.00       "                          98 

24.0 

97 

2.7 

oh.  55m. 

I  380 

79 

6571 

"       22 

11.00       "                          98 

24.0 

97 

3-o 

ih.  55m. 

2  82O 

128 

6572 

"       22 

12.  OO       "                          98 

23-5 

95 

3-2 

2h.  55m. 

4240 

149 

6573 

"       22 

I.OO  P.M.                       98 

23-5 

95 

3-6 

3h.  55m. 

5640 

194 

6574 

"       22 

1.  10       "                          98 

23-5 

95 

4h.  osm. 

5870 

241 

Closed  outlet  at  1.12  P.M. 

6575 

"       22 

3-13     "                   99 

oh.  osm. 

148 

35° 

6576 

"       22 

3.18     "                   99 

20.  o 

81 

oh.  lorn. 

253 

265 

£>577 

"       22 

3-23     " 

99 

23-5 

95 

oh.  ism. 

378 

33° 

6579 

"       22 

3-38     " 

99 

23-5 

95 

oh.  3001. 

738 

189 

6580 

"       22 

4.00     " 

99 

23-5 

95 

2.6 

oh.  4401. 

1068 

233 

6581 

"       22 

5-3°     " 

99 

23-5 

95 

4.0 

2h.  14111. 

3098 

82 

6582 

"       23 

1.30  A.M. 

101 

23-5 

95 

2-5 

oh.  o6m. 

168 

269 

6583 

"       23 

1-35     " 

101 

23-5 

95 

oh.  nm. 

248 

265 

6584 

!     23 

1.40     " 

101 

24.0 

97 

oh.  i6m. 

368 

255 

6585 

1.50     " 

101 

23-5 

95 

oh.  26m. 

578 

1  80 

6586 

"     23 

2.00       " 

101 

23-5 

95 

2-7 

oh.  3601. 

888 

173 

Closed  outlet  at  2.07  A.M. 

6588 

"     23 

4.17       ' 

102 

23-5 

95 

oh.  osm. 

119 

297 

6589 

"    23 

4-23       " 

102 

20.0 

81 

oh.  nm. 

239 

415 

6590 

"    23 

4.30       "                        102 

23-5 

95 

2.  I 

oh.  i8m. 

419 

274 

6591 

:'    23 

5.00       " 

IO2 

23-5 

95 

2.4 

oh.  4Sm. 

1099 

295 

6592 

"     23 

5-30       " 

102 

23-5 

95 

2.6 

ih.  i8m. 

1789 

272 

"593 

"     23 

6.00     "                  102 

23-5 

95 

2-7 

ih.  4sm. 

2469 

268 

G594 

"     23 

8.00-  "                 102 

23-5 

95 

3-0 

3h.  lorn. 

4379      261 

Closed  outlet  at  8.10  A.M. 

6595 

;<     23 

2.40    P.M.                    103 

oh.  osm. 

I2O         TC7 

6596 

"     23 

2-45     "                103 

24.0 

97 

oh.  lorn. 

240 

136 

6597 

"     23 

2.50   " 

103 

23-5 

95 

oh.  ism. 

370 

142 

6599 

"     23 

3.00    " 

103 

23-5 

95 

2-7 

oh.  25m. 

630 

161 

6600 

"     23 

3.30   •' 

103 

23-5 

95 

2.8 

oh.  55m. 

I  360 

187 

6601 

"    23 

4-35     ' 

103 

23-5 

95 

2h.  oom. 

2  860 

272 

Closed  outlet  at  4.35  P.M. 

6602 

"    23 

6.00     " 

104 

23-5 

95 

2.0 

oh.  i6m. 

374 

153 

6603 

"     23 

8.00     " 

104 

23-5 

95 

2-9 

2h.  I4m. 

3274 

45 

6605 

'    23 

8.30     " 

104 

23-.S 

95 

2.9 

2h.  44m. 

4014 

41 

6606 

'    23 

9.30     " 

104 

23   5 

95 

3-1 

3h.  44m. 

5434 

86 

6607 

'    23 

10.30     " 

104 

23-5 

95 

3-3 

4h.  44m. 

6854 

181 

6608 

'    23 

11.30     " 

104 

23-5 

95 

3-5 

5h.  44m. 

8  284 

212 

Closed  outlet  at  11.35  P.M. 

6628 

'    24 

2.13     " 

107 

20.0 

81 

oh.  osm. 

133 

230 

6629 

'    24 

2.18     " 

107 

21.0 

85 

oh.  lorn. 

273 

l6q 

6630 

'    24 

2.23     " 

107 

21.  O 

85 

oh.  ism. 

378 

147 

6632 

'    24 

3  .  oo     " 

107 

2O.  O 

81 

2.0 

oh.  52m. 

I  168 

151 

6633 

'    24 

4.00     " 

107 

20.0 

81 

2.2 

ih.  52m. 

2388 

825 

Closed  outlet  at  4.10  P.M. 

6637 

'    24 

9.11      ' 

109 

18.0 

73 

oh.  osm. 

76 

605 

6638 

'    24 

9.16     " 

109 

18.0 

73 

oh.  lorn. 

166 

625 

6639 

"    24 

9-3°     " 

109 

18.0 

73 

oh.  24111. 

406 

580 

Closed  outlet  at  9.34  P.M. 

INVESTIGATIONS  OF  THE  WATER  COMPANY  FROM  APRIL  TO  JULY,  1807.    355 


RESULTS    OF    BACTERIAL   AN ALYSES— WITH    SULPHATE   OF    ALUMINA.— Continued. 


k.,i,  ol 

~ 

8 

Collected. 

Filtration. 

ii. 

in  . 

- 

t 

Number 

I 

i& 

•a 

Period  of 

u  ** 

3 
(j  . 

E 
iz 

Date. 

Hour 

of   i  5 
un.   ;  £2 

Hi 

K 

Washing. 
Hours  and 
Minutes. 

^|^ 

"  *".5 

t|              Remarks. 

•2 

|| 

=  0.3"  Z 

-23 

rtW 

& 

u 

S, 

J 

ta 

n 

1897 

6687 

June  26 

9.30  P.M. 

116 

23-5 

95 

2.2 

oh.  o6m. 

145 

127 

6688 

"  26 

9-35  " 

116 

23-5 

95 

oh.  nm. 

245 

73 

6689 

"  26 

9-45  " 

116    23.5 

95  •••• 

oh.  i6m. 

555 

81 

6690 

"  26 

o.oo  " 

116    23.5 

95 

2-3 

oh.  3&m. 

865 

39 

6691 

"  26 

O.2O   " 

116    23.5 

95 

oh.  56111. 

i  295 

89  Closed  outlet  at  10.21  P.M. 

6692 

"  27 

2.20  A.M. 

"7    23.5 

95 

oh.  O7m. 

207 

86 

6693 

"  27 

2.30   " 

"7    23-5 

95 

2.2 

oh.  I7m. 

447 

51 

6694 

"  27 

2.45   ' 

"7    23.5 

95 

oh.  32m. 

745 

77 

6695 

"  27 

1.  00   " 

"7    23.5 

95 

2.0 

oh.  47m. 

i  147 

99  Closed  outlet  at  1.04  A.M. 

6697 

"  27 

3.00  " 

nS    23.5 

95 

2.O 

oh.  O5m. 

1=6 

580 

6698 

"  27 

3.15  " 

118   23.5 

95 

oh.  2Om. 

456 

3800 

Closed  outlet  at  3.15  A.M. 

6726 

"  28 

3.50  •' 

124  ;  23.5 

95 

oh.  05111. 

122 

6727 

"  28 

3-55  " 

124 

23.5 

95 

oh.  lorn. 

242 

<>--- 
6729 

"  28 
"  28 

4.00  " 
4-30  " 

124 
124 

23-5 

23-5 

95 
95 

2-5 

oh.  i5m. 

oh.  45m. 

342 
I  052 

880 

Closed  outlet  at  4.30  A.M. 

6730 

"  28 

8.00  " 

125 

23.5 

95 

2.5 

oh.  54m. 

I  263 

29 

6732 

"  28 

9.00  " 

125 

23-5 

95 

2.3^  ih.  54tn. 

2663 

26 

6733 

"  28 

0.30  " 

125 

23.5 

95 

3.01  3h.  24m. 

4763 

20 

6734 

"  28 

2.00  M. 

125 

23.5 

95 

3.7   4h-  54m. 

6853 

32 

6735 

"  28 

2.  GO  P.M. 

125   23.5 

95 

3.9   6h.  54tn. 

9653 

39 

6737 

"   29 

0.47   ' 

126 

23-5 

95 

oh.  osm. 

152 

372 

6738 

"   29 

0.51   ' 

126 

23.5 

95 

oh.  urn. 

252 

163 

6739 

"   29 

1.02   " 

126   23.5 

95 

oh.  22m. 

522 

204 

6740 

"   29 

1.24   " 

126 

23-5 

95 

oh.  44m. 

992 

256 

6741 

"  30 

2.30  A.M. 

126 

23-5 

95 

2.6 

ih.  5001. 

2  532 

269 

6742 

"  3° 

I  30  " 

126 

23.5 

95 

2-7 

2h.  5om. 

3882 

i  250 

'>7t  i 

"  3° 

2.30   " 

126 

23.5 

95 

3-o 

3h.  som. 

5  262 

9i 

6745 

"  3« 

3-30   " 

126 

23-5 

95 

3-4 

4h.  50tn. 

6682 

49 

6746 

"  30 

4.30   " 

126 

23-5 

95 

3-5 

5h.  som. 

8  112 

92 

6747 

"  30 

5.30   " 

126 

23-5 

95 

3-7 

6h.  5om. 

9492 

94 

6749 

"  3° 

9-00   " 

127 

23-5 

95 

2.  I 

oh.  5im. 

I  232 

127 

6750 

"  3° 

9.30   " 

127 

23.5 

95 

ih.  2im. 

I  891 

26 

Closed  outlet  at  9.35  A.M. 

6763 

"  30 

8.IO  P.M. 

130 

23-5 

95 

oh.  o6m. 

150 

119 

6764 

"  3° 

8.15  " 

130 

23-5 

95 

oh.  Iim. 

250 

69 

6765 

"  3° 

8.25  " 

130 

23-5 

95 

oh.  2im. 

500 

59 

6766 

'  3° 

8.45  " 

130 

23.5 

95 

oh.  4lm. 

I  OOO 

84 

6771 

"  3° 

IO.OO   " 

130 

23.5 

95 

2.6 

ih.  5&m. 

2750 

61 

6772 

"  3° 

11.00   " 

130 

23-5 

95 

2.8 

2h.  56m. 

4130 

34 

6773 

'  30 

12.  OO   " 

130 

23.5 

95 

2-9 

3h.  s6m. 

5470 

too 

6774 

July  i 

1.  00  A.M. 

130 

23.5 

95 

3-2 

4h.  56111. 

6870 

84 

^775 

'  '   i 

2.OO   '  ' 

i  ^o 

nc 

8  270 

6776 

1  '   I 

3.OO   '  ' 

i  j\j 
130 

23.  5 

OO   £ 

ys 

nc 

3  -4 

37 

6h.  56m. 

9610 

6778 

"   I 

5.41   " 

131 

*  J  '  J 
23-5 

VD 

95 

•  I 

oh.  o6m. 

142 

81 

6779 

"   I 

5-47   " 

131 

23-5 

95 

oh.  I2m. 

242 

39 

6780 

"   I 

5-57   " 

131 

23-5 

95 

oh.  22m. 

492 

8 

6784 

"   I 

6.19   " 

131 

23.5 

95 

oh.  44m. 

992 

68 

6785 

"   I 

8.00  " 

131 

23-5 

95 

2-7 

2h.  25111. 

3  262 

84 

<7-7 

"   I 

9.00  " 

131 

23-5 

95 

3-o 

3h.  25m. 

4662 

23 

<>:-- 

"   I 

10.00   " 

131 

23-5 

95 

3-2 

4h.  25m. 

6042 

25 

6789 

'  '   1 

1  1  .00  " 

1  1  1 

2T   C 

QC 

37 

5h.  25m. 

7  jio 

6824 

"    2 

5.00  P.M. 

1  J  * 

136 

*-j  •  3 

23-5 

V3 

95 

•  / 
2.O 

oh.  04m. 

/  <*•+* 
IO9 

67 

6825 

"    2 

5.30   " 

136 

23.5 

95 

oh.  34m. 

809 

6826 

"    2 

7.30   " 

136  |  23.5 

95 

29 

2h.  34m. 

3519 

20 

6827 

"    2 

8.30   " 

136 

23.5 

95 

3-7 

3h.  34rn. 

4869 

18 

6832 

"    2 

9-30   " 

136 

23.5 

95 

4-3 

4h.  34m. 

6259 

57 

f..s3;, 

"    2 

10.30   " 

136 

23-5 

95 

4-5 

5h.  34m. 

7649 

61 

1,831 

"    2 

11.30   " 

136 

23.5 

95 

4.6 

6h.  34m. 

8999 

22 

6835 

"   3 

1.  00  A.M. 

136 

23.5 

95 

5-o 

8h.  04111. 

II079 

21 

6837 

3 

3.02   " 

137 

23-5 

95 

oh.  07111. 

142 

99 

(,S;, 

3 

3-05   " 

'37 

23-5 

95 

oh.  lorn. 

242 

87 

6839 

3 

3-22   " 

137   23.5 

95 

oh.  27m. 

602 

66 

',-.('! 

3 

4.00   " 

137   23-5 

95 

ih.  osm. 

I  502 

26 

6841 

3 

5-00   " 

'37  ;  J3-5 

95 

3  o 

2h.  osm. 

2  842 

3i 

6845 

3 

6.00  " 

137   23-5 

95 

3-8 

3h.  osm. 

4252 

25 

35' 


WA  TEK   P  URIFICA  TION  AT  LO  UIS  VI L  L  E. 


RESULTS   OF    BACTERIAL    ANALYSES— WITH    SULPHATE    OF   ALUMINA.— Continued. 


Rate 

of 

j 

i. 

Collected. 

Filtrat 

on. 

fc 

i/i  u          -° 

£ 

Number 

8. 

i 

Period  of 

i.E    .          U    . 

Run. 

K 

Last 
HouSrsTnRd 

g||          ||    j                              Remarks. 

x 

Date. 

Hour. 

£§  =<J 

u  c        O  ^-C 

0 

Minutes. 

•2 

".35       i: 
3«=i 

=  a? 

i 

^JU          |(J 

J) 

u 

5 

-> 

U.              :        03 

1897 

6846 

July    3 

8.OO  A.M. 

137 

23-5 

95 

4.8 

5h.  «5m. 

7  022        39 

6848 

3 

g.OO      " 

137 

23-  5: 

95 

5.5 

6h.  0501. 

8412        72 

6859 

"       6 

1.30  P.M. 

140 

230 

95 

2.2 

oh.  lom. 

272      291 

6860 

6 

1-45       " 

140 

23-5 

95 

2-5 

oh.  25m. 

652        98 

6861 

6 

2.3O      " 

140 

24.0 

97 

2-5 

ih.  lom. 

i  692        47 

6863 

"       6 

4.00      " 

140 

23-5 

95 

2-9 

2h.  4om. 

3  792        62 

6865 

6 

5-30      " 

140 

23-5 

95 

3-5 

4h.  lom. 

5912        41 

6866 

6 

8.30      " 

140 

23-5 

95 

4.8 

7h.  lom. 

10  192        49 

(,S()7 

"       6 

9.00      " 

140 

23-5 

95 

5.0      7h.  40m. 

10  902        33 

6870 

"       6 

10.00        " 

140         23.5 

95 

5.6      Sh.  40111. 

12282        38 

6871 

6 

I  I  .  OO       " 

140         23.5 

95 

6.oj     gh.  40111. 

13622        37 

6872 

"       6 

12.00       " 

140 

23.5 

95 

6.9    loh.  40tn. 

14972        31 

6873 

"       7 

1.  00  A.M. 

140 

23-5 

95 

7.5    nh.  40m. 

16  322        92 

6874 
6876 

7 
7 

2.OO       " 
3.00       " 

140         23.5 
140         23.5 

95 
95 

7-S    i2h.  4om. 
8.3    I3h.  4om. 

17  602 
18  912 

126 
49    Agitated  surface  of  sand  layer  at 

6877 

7 

4.00       " 

140         23.5 

95 

5.2    i4h.  32m. 

20022          58 

3.37  A.M. 

6878 

"       7 

5.OO       " 

140         23.5 

95 

5.7    ish.  3201. 

21  3,2 

in 

6879 

7 

6.00     " 

140         23.5 

95 

6.6    i6h.  32m. 

22  522 

143 

6881 

7 

9.00     " 

140         23.5 

95 

7.6 

I9h.  28m. 

26  592 

405  .Closed  outlet  at  9.03  A.M. 

6882 

7 

10.24     "                 141         23.5 

95 

oh.  osm. 

146 

33« 

6883 

7 

10.30     "                 141        23.5 

95 

2.1 

oh.  urn. 

286 

295 

6885 

11.00     "                 141         23.5 

95 

2-3 

oh.  41  m. 

I  OO8 

200 

Closed  outlet  at  11.13  A-M- 

(,ssi 

"       7 

11.46     ' 

142         23.; 

95 

2-3 

oh.  o6m. 

I48 

195 

6887 

7 

11.51      " 

I42          23.5 

95 

oh  .  1  1  m  . 

258 

I56 

68  SS 

7 

12.00  M. 

142         23.5 

95 

2.  I 

oh.  2om. 

478 

156 

6889 

7 

1.  00    P.M. 

142 

23-5 

95 

2-9 

ih.  2om. 

928 

61 

6890 

7 

2.OO       " 

142         23-5| 

95 

3-7 

2h.  2om. 

3313 

98 

6892 

7 

2.30       " 

142         23.0 

93 

3-8 

2h.  som 

4008 

144 

Closed  outlet  at  2.39  P.M. 

6893 

7 

3-5()       " 

143 

23.5 

95 

2.  I 

oh.  o6m 

148        320 

6894 

7 

4.OO       " 

'43 

23-5 

95 

2.1 

oh.  lom 

238        305 

6897 

7 

4.11      " 

U3    ;  23.5 

95 

oh.  24111 

498 

282 

6898 

7 

4,3"     " 

143       23.5 

95 

2.  2 

oh.  4om 

948 

259 

6899 

7 

5-30     " 

143    i  23.5; 

95 

2-3 

ih.  4om 

1663 

191 

6901 

7 

9-32     " 

M4 

23-5 

95 

oh.  o6m 

141 

310 

6902 

7 

9-36     " 

M4 

23-5 

95 

oh.  lom 

241 

242 

690; 

7 

9.48     ' 

M4 

23-5i 

95   !•••• 

oh.  22m 

471      625 

6905 

7 

10.30     " 

144 

23-5 

95 

2.7 

ih.  04111 

1481 

133 

6gof 

7 

I  I  .  OO       " 

M4 

23-5 

95 

2-9 

ih.  34111 

2  171 

192 

6907 

"       7 

11.30     "                 144 

23.5 

95 

2h.  04111 

2S7I 

182 

Closed  outlet  at   11.35  P.M. 

6qoS 

"       8 

12.54  A.M. 

145 

23-5 

95 

oh.  07111 

145 

261 

6909 

"       8 

I  .  OO       " 

M5 

23-5 

95 

2.0 

oh.  13111 

275 

198 

6910 

S 

1  .  30       " 

M5 

23-5 

95 

2.1 

oh.  43m. 

965 

174 

6qi 

"       8 

2.00       " 

M5 

23-5 

95 

2.1 

ih.  13111. 

i  535 

82 

69  1  . 

"       8 

4.00       " 

145 

23.5 

95 

2.2 

3h.  1301. 

4375 

61 

691; 

S 

5.00       " 

145 

23-5 

95 

2-7 

4h.  13111. 

5725 

68 

691 

"       S 

6.00     " 

M5 

23-5 

95 

2.g 

5h.  13111. 

7°55 

69 

691 

"       8 

9.00     " 

M5 

23-5 

95 

3-6 

8h.  I3m 

it  245 

147 

Closed  outlet  at  9.15  A.M. 

692 

"       S     i          10.03     " 

146 

23-5 

95 

oh.  06  m 

151 

245 

692 

8 

10.12      " 

146 

23-5 

95 

oh.  1  5m 

37' 

260 

692 

"       S 

11.30    '• 

146 

23-5 

95 

2.2 

ih.  33m 

2  igl 

138 

692 

"       8 

I.OO  P.M. 

146 

23-5 

95 

2-7 

3h.  03111 

4281 

152 

692. 

8 

2.30     " 

146 

23-5 

95 

2-? 

4h.  3301 

6321 

MS 

694 

9 

4.52    ' 

149 

23-5 

95 

oh.  07m 

251 

305 

694 

9 

5.00    " 

149 

23-5 

95 

2.2 

oh.  ism 

381 

127 

694 

9 

8.00     " 

149 

23-5 

95 

2.8 

3h.  ism 

4751 

56 

694 

9 

9.00     " 

149 

23-5 

95 

2.r 

4h.  I5m 

6171 

61 

6g66|      "     10 

4.40A.M.              153 

23.5 

95 

oh.  osm 

M<>!     U7 

696- 

"        TO 

4.45    '             153 

23-5 

95 

oh.  jom 

24f 

67 

696c 

"       10 

5.30   "           153 

23-5 

95 

2.: 

oh.  46111 

i  036 

64 

6g7( 

)            '       10 

6.00     "                 153 

23-5 

95 

2.-1 

ih.  i6m 

I  746 

60 

697 

"       10 

S.oo     "                 153 

23-5 

95 

2.1 

3h.  i6m 

4616 

295 

697: 

"        10 

9.00     "                 153 

23.5 

95 

3-( 

4h.  i6m 

6036 

70 

697 

"       10 

10.00     "                 153 

23.5 

95 

3-c 

5)1.  1  6m 

7436 

72 

Closed  outlet  at  10.05  A.M. 

698 

'       10 

5.24  P.M.                    156 

23-5 

95 

oh.  o6m 

I5C 

171 

INVESTIGATIONS  OF  THE  WATER  COMPANY  FROM  APRIL   TO  JULY,  18H7.    357 


RESULTS    OF    HACTERIAL    ANALYSES— WITH    SULPHATE    OF    ALUMINA.  —  Continued. 


( 

Elected. 

s 
a 

7. 

Date. 

Hour. 

1 

6986 

1897 
July  10 

5.32  P.M. 

6987 

"   10 

5.40   " 

6992 

;;  M 

8.55  " 

6993 

8.59  " 

6994 

"   T4 

9.10  " 

6995 
6998 

::  11 

9.30  " 

O.GO 

6999 

'  !4 

1.23   " 

7000 

"  14 

1.27   " 

7003 

"  M 

I.38   " 

7004 

"  M 

2.OO   " 

7006 

"  15 

4.49  A.M. 

7007 

'   15 

4-53   " 

7010 

'  15 

5.04   ' 

7011 

'  J5 

5-30   " 

7012 

'  15 

6.00  " 

7013 

'  15 

S.oo  " 

7015 

'  15 

9.00  " 

7018 

'  15 

0.06  " 

7019 

'  15 

o.io  •' 

7022 

'  15 

0.30  " 

7023 

'  15 

1.30 

7024 

'   15 

2.30  P.M. 

7025 

'   15 

2.52   ' 

7026 

'   15 

3.OO 

7030 

'   15 

3-30  " 

7°3' 

'  '15 

4.30  " 

7032 

'  15 

8.00  " 

7036 

'  15 

9.00  " 

7°37 

'   15 

o.oo  " 

7038 

'   15 

1.16  " 

7039 

'  15 

i  .  20  " 

7040 

'  15 

1.30 

7043 

'  15 

2.OO 

7044 

"  16 

I.OO  A.M. 

7046 

"  16 

3-5f>  " 

7047 

"  16 

4.00 

7<>49 

"   16 

5.00 

7050 

"   16 

6.00  " 

7052 

1   16 

9.00  " 

7«53 

"  16 

10.17  "  ' 

7054 

"   16 

10.22   " 

7055 

"   16 

11.00   " 

7"57 

"   if. 

12.  OO  M. 

7058 

"   16 

I.OO  P.M. 

7061 

•   16 

9.58   " 

7062 

"  16 

IO.O2   " 

7064 

"   16 

10.12   " 

7065 

"   If) 

11.00   " 

7066 
7067 

"   '6 

"   17 

12.00   " 
I.OO  A.M. 

7068 

'   17 

2.00   " 

7070 

'  17 

4.14   " 

7071 

'  17 

4.18   " 

7072 

'  17 

4.30   " 

7"75 

'  17 

S.oo  " 

7076 

'  17 

6.  oo  " 

7°77 

'   17 

8.00  " 

7079 

'   17 

9.00  " 

7080 

"   r~ 

IO.OO   " 

7081 

"  17 

II.  OO   " 

7082 

'   '7 

12.00  M. 

•,-083 

'  17 

I.OO  P.M. 

7084 

'  17 

2.OO   " 

Rate  of           S 

s 

Filtration.         £ 

1  . 

~ 

lumber 

V                 C   V 

o.        _o  a    i    -o 

Period  of 

«.S  • 

u  . 

Last 

>  S  « 

a." 

Remarks. 

Run. 

Si  v      G  5  3      I 
[1.5       j-<  o  :    _ 

HWouVs^d 

r*  .      [i, 
-c!-~    y 

8 

Minutes. 

V   3^ 

S  £ 

•^  IS      S  :£  cT      § 

~,J;j 

"u 

u        S       j    J 

£ 

e 

I56 

23.5      95     

oh.   14111. 

300 

192 

156 

23-5      95 

oh.  22m. 

500                 72 

157 

23-5      95 

oh.  o6m. 

150            193 

157 

23.5      95     ••• 

oh.  lom. 

250            251 

157 

23-5      95     •••• 

oh.  2im. 

500            340 

157 

23.5      95   ;   2.2 

oh.  4im. 

96O             l82 

157 

23.5      95     

ih.  urn. 

i  f'55      143 

Closed  outlet  at  10.01  P.M. 

158 

23.5      95     .... 

oh.  o6m. 

148      244 

158 

23-5      95 

oh.  lom. 

248      225 

158 

23-5      95 

oh.  2im. 

498      217 

I5S 

23-5      95 

2-3 

oh.  43m. 

998      229 

Closed  outlet  at  12.03  A.M. 

'59 

23-5      95     --- 

oh.  lom. 

254,     260 

159 

23-5      95     •--. 

oh.  14111. 

354 

274 

159 

23.5      95     

oh.  25m. 

5M 

177 

159 

23-5      95      2.2 

oh.  5im. 

i  294 

230 

159 

23.  5      95      2.4    ih.  aim. 

i  884 

M5 

159 

23-5      95      2.7    3h.  2irn. 

4  634 

96 

'59 

23-5      95      3-3    4h-  2irn. 

5984 

138 

Closed  outlet  at  9.18  A.M. 

1  60 

23.5      95     oh.  o()in. 

150 

122 

1  60 

23  -5 

95 

oh.  lom. 

250 

84 

1  60 

24.0 

97 

2-3 

oh.  30111. 

730 

74 

1  60 

23-5 

95 

3.0    ih.  3om. 

2   HO 

80 

1  60 

23-5      95      3-7    2h.  30111. 

347° 

88 

161 

23.5      95     ....     oil.  06111. 

'43 

96 

161 

23-5      95 

2.3    oh.  14111. 

363 

86 

161 

23-5      95 

2.6    oh.  44m. 

i  063 

177 

161 

23-5 

95 

3.2    ih.  44111. 

2573 

88 

If.2 

23-5 

95 

2.2     ih.   30111. 

2059 

1  66 

162 

23-5      <_>5 

2.6    2h.  30111. 

3419 

3! 

-.62 

23-5      95 

3.0    3h.  30111. 

4799 

73 

Closed  outlet  at  10.00  P.M. 

163 

23-?       95 

oh.  o6m. 

149 

59 

1  63 

23.5 

95 

oh.  torn. 

249 

38 

163 

23-5 

95 

•j.  i 

oh.  2om. 

499 

34 

163 

23-5 

95 

oh.  5orn.   :     I  159 

48 

163 

23-5 

95 

2.,) 

ih.  50m.   ;    2  539 

43 

164 

23-5 

95 

oh.  o6m.   '        148 

Si 

\ 

164 

23.5 

95 

2.  I 

oh.  torn.           232 

92 

164 

23-5       95 

2.2    ih.  loin.        I  628 

49 

164 

24.0     97 

2.5    2h.  lom.        3078 

65 

165 

23-5      95 

2.3    oh.  46111.        i  098 

128 

Closed  outlet  at  9.04  A.M. 

1  66 

23-5      95 

oh.  0501.           151 

55 

1  66 

23-5 

95 

oh.  lom.   ]       251 

57 

1  66 

23-5 

95 

2-4 

oh.  48m.        i  161 

37 

1  66 

23-5 

95 

2.6 

ih.  48m.   :    2  561 

3" 

166 

23-5 

95 

2-9 

2h.  48111.        3  991 

98 

Closed  outlet  at  1.12  P.M. 

167 

23-5 

95 

oh.  o6m.   |        142 

63 

167 

23-5 

95 

oh.  lom.   i       242 

5' 

167 

23-5 

95 

oh.  2om     !       492 

55 

167 

23-5 

95 

2.3 

ih.  oSm.    i     i  572 

37 

167 

23-5 

95 

2.9     2ll.   08  111.          3  022 

26 

167 

23-5 

95 

3.0 

3h.  o8m.       4  352 

33 

167 

23-5 

95 

3-  2 

4h.  o8m.        5  582 

25 

168 

23-5 

95 

oh.  07111.           146 

23 

168 

23-5 

95 

oh.  urn.          246 

17 

168 

23.5 

95 

2.2 

oh.  23m.           536 

14 

168 

23-5 

95 

2-3 

oh.  5301.        I  236 

u 

1  68 

23-5 

95 

2.51   ih.  53111.       2666 

27 

1  68 

23.5 

95 

2-9    3h.  53m.       5456. 

7 

168 

23-5 

95 

3.1    4h.  53111 

6876 

31 

1  68 

23.0 

93 

3.6    sh.  53m. 

8266 

22 

168 

23-5 

95 

3.8    6h.  5301. 

9  666 

19 

168 

23-5 

95 

3-9    7h.  53m. 

1  1  086 

37 

if.8 

23.0 

93 

4.0    8h.  5301. 

12456 

49 

1  68 

23-5 

95 

4-4 

9h.  53111. 

13856 

72 

358 


WATER   PURIFICATION  AT  LOUISVILLE. 


RESULTS    OF    BACTERIAL    ANALYSES— WITH    SULPHATE    OF    ALUMINA.— Continued. 


Rate  of 

j 

8 

Collected. 

Filtration. 

EL. 

c 

« 

. 

—  u    t/nr 

Period  of   "  <*> 

3 

V 

Number   5. 

C  P. 

_^  Service  Since  i-s*j 

u  ^ 

1 

5  "  " 

a 

Washmf?.   £j| 

11  i! 

Remarks. 

X  ,    Date. 

Hour. 

fe  5 

c  <  c 

Hours  and   -ol*  u 

.£•- 

u  C 

o  ,_  X 

° 

Minutes.    L.  w!5 

V  C 

& 

Is 

U 

|c.S 

S         z36 

9? 

1897 

7090  July  17 

5.13  I'.M. 

169   23.5 

95 

oh.  0701.    153 

12 

7cgi    '  17 

5.30   " 

169  23.5 

95 

2.1   oh.  22m.    563 

23 

7094    '  i? 

7.30   " 

169 

23-5 

95 

2.g   2h.  22tn.  3433 

35 

7095    '  T  7 

8.30   " 

i6g    23.5 

95 

3.1   3h.  22m.  4763 

14 

7097    '  17 

9.30   " 

169   23.5 

95 

3.7!  4h.  22m.  6  113 

19 

7098    '  17 

II.OO   " 

i6g    23.5 

95 

4.6   sh.  52m.  S  253 

7 

7099    '  17 

12.00   " 

169    23.5 

95 

4-g   6h.  52m.  9693 

13 

7102    '  18 

I.OO  A.M. 

169 

23-5 

95 

5.3   -h.  52m. 

n  403 

30 

7103   "  18 

2.00   " 

i6g 

23.5 

95 

5.6 

Sh.  52m. 

12  503 

32 

7105    '  18 

3.00   "          169    23.5 

95 

5.8   gh.  52111.  13  Sg3 

44 

Closed  outlet  at  3.07  A.M. 

7106    '  18 

4-50   "          170    23.5 

95 

oh.  osm.    134 

36 

7107   "  18 

5.00  "       170   23.5 

95 

2.  I 

oh.  15111.    374 

17 

7108   "  18 

5.30  "      170   23.5 

95 

2.1   oh.  45m.   i  054    20 

7109   "  18 

6.00  " 

170  :  23.5 

95 

2.2   ih.  15111.   i  744 

13 

7113   "  18 

g.oo  " 

i/o    23.5 

95 

2.4 

4h.  ism.;  5  954 

29 

7116    '  18 

11.00  "        170    23.5 

95 

3.7   6h.  ism.  8  754 

ii 

7117   "  iS 

I.OO  P.M.        170    23.5 

95 

4.  i   Sh.  15111.  11-544 

14 

7119   "  18 

3.00  " 

170   23.5 

95 

4.8  ioh.  ism.  14  344 

26 

7120   "  IS 

4.00  " 

170   23.5 

95 

5.0  iih.  ism.  15  754 

Si 

Closed  outlet  at  4.06  P.M. 

7121    "  18 

5.22  " 

171    23.5 

95 

....   oh.  o6m.    150 

15 

7122'   "  18 

5.30  " 

171  '  23.5 

95 

2.1   oh.  1401.    340 

19 

7125  "  is 

8.00  " 

171    23.5 

95 

2.8   2h.  44m.  3  910 

18 

7126   "  18 

9.00  " 

171 

23-5 

95 

3h.  44m.  _5  270 

4 

7128   "  IS 

10.00   " 

171 

23-5 

95 

3.8;  4h.  44m.  6  610 

5 

7129    '  18 

II.OO   " 

171    23.5 

95 

4.2   sh.  44m.   8030 

2 

7130    '  18 

12.  OO   " 

171    23.5 

95 

4.8   6h.  44m.  9  450 

3 

7133    '  19 

I.OO  A  M. 

171  '  23.5 

95 

5-2 

7h.  44m.  10  890 

21 

7134    '  19 

2.OO   " 

171    23.5 

95 

5.7   Sh.  44tn.  12  320 

26 

7136    '  19 

3.00   "          171 

23-5   95 

5.9   gh.  44m.  13  730 

36 

71.37    '  19 

4.OO   " 

171    23.5 

95 

6.2 

ioh.  44111.  15  130 

124 

7138    '  19 

8.56   " 

172  :  23.5 

95 

.  .  .  .   oh.  06111.    151 

14 

7140    '  ig 

g.oo_  " 

1/2    23.5 

95 

2.2:  oh.  lorn.    286 

21 

7141    '  19 

10.00'  " 

172  i  23.5 

95 

2.4   ih.  torn. 

1686 

2 

7M4    '  19 

12.  OO  M. 

172    23.5 

95 

2.9:  3(1.  torn. 

4  526'    7 

7M5    '  19 

2.00  P.M. 

172 

23.5 

95 

3.4   sh.  ion). 

7  326[    8 

7147^   '  19 

3-30  " 

172 

23-5 

95 

3.6 

6h.  40111. 

9  456 

5 

7148    '  19 

5.00  " 

172 

23-5 

95 

4.0   Sh.  lorn. 

II  536 

18 

7M9 

'   19 

7.30  " 

172 

23.5 

95 

4.7  ioh.  40111. 

15  066 

in 

Closed  outlet  at  7.49  P.M. 

7i5i 

'   19 

9.09  " 

1/3 

23-5 

95 

...   oh.  o6m. 

150 

52 

7152 

ig 

9-13  ' 

173 

23-5 

95 

.  .  .  .   oh.  lorn. 

250 

26 

7155 

"   19 

9.30  " 

173 

23.5 

95 

2.  I 

oh.  27m. 

650 

43 

7156 

'   19 

10.  OO   " 

173 

23-5 

95 

2.  I 

oh.  57m. 

i  370 

32 

7'57    '  19 

10.30  " 

173 

23.5 

95 

2.2 

ih.  27m. 

2  070 

49 

7158    '  19 

12.  OO   " 

173 

23-5 

95 

2.3   2h.  57111. 

4  i  So 

36 

7161 

;'   20 

I.OO  A.M. 

173 

23.5 

95 

2.4   3h.  57m. 

5580 

21 

7162 

"   2O 

3.00  " 

173 

23-5 

95 

2.7   sh.  57111. 

8390 

30 

7164 

"   20 

5.00  " 

173 

23.5 

95 

2.9 

7h.  57m. 

10  090 

27 

7167 

"   20 

6.00  " 

173 

23-5 

95 

9h.  57m. 

12  5OO 

31 

7168 

"   2O 

8.00  " 

173 

23-5 

95 

3-5 

ioh.  57m. 

15  300 

23 

7170 

"   20 

IO.CO   " 

173 

23-5 

95 

3-7 

I2h.  57m. 

18  ioo 

31 

7171 

"   20 

12.  OO  M. 

173 

23-5 

95 

3-9 

I4h.  57m. 

20950 

25 

7172 

"   20 

2.00  P.M. 

173 

23.5 

95 

4-  1 

i6h.  57m. 

23  780 

28 

7174 

"   20 

3-30  " 

173 

23-5 

95 

4-3 

i8h.  37m. 

25900 

31 

7177 

"   20 

5.00  " 

173 

23-5 

95 

4.8 

igh.  57m. 

28  990 

33 

7178 

"   20 

8.00  " 

173 

23-5 

95 

5-0 

22h.  57m. 

32  ioo 

3° 

Closed  outlet  at  8.04  P.M. 

7180 

"   20 

9.15  " 

174 

23-5 

95 

oh.  o6m. 

153 

21 

7181 

"   20 

9.19  " 

174 

23-5 

95 

oh.  lorn. 

253 

27 

7182 

"   2O 

9.30  " 

174 

23-5 

95 

2.2 

oh.  2im. 

493 

21 

7183 

"   20 

10.00  " 

174 

23-5 

95 

2.2 

oh.  51  m. 

i  173 

7i85 

"   20 

II.OO   " 

174 

23-5 

95 

2-5 

ih.  sim. 

2573 

41 

7186 

"   2O 

12.00   " 

174 

23-5 

95 

2.8,  2h.  5im. 

3953 

39 

7187 

"   21 

I.OO  A.M. 

174 

23-5 

95 

3.0   3h.  Sim. 

5373 

25 

7188 

"   21 

2.OO   " 

174 

23.5 

95 

3.2;  4h.  Sim. 

6612 

16 

7190 

"   21 

3.30  " 

174 

23-5 

95 

4.  i|  6h.  2im. 

8613 

12 

INVESTIGATIONS  OF  THE  WATER  COMPANY  FROM  APRIL   TO  JULY,  1897.  359 


RESULTS    OF    BACTERIAL    ANALYSES— WITH    SULPHATE    OF    ALUMINA.-  Concluded. 


Rat 

;  of 

5 

s 

:ollccted. 

Kiltra 

lion. 

£ 

Ji 

lo 

• 

k. 

tr.  u 

Period  of 

u  "* 

3 

1 

Number 

0. 

1  °- 

•a 

ServiceSince 

ii--  J 

u 

s 

of 

M 

"rt  v  "> 

S 

Last 

>  "£  1J 

V  M 

Remarks 

Run. 

flj  V 

C  5j  -• 

X 

Washing. 

J>^ 

«  i 

•S. 

Date. 

Hour. 

u.  - 

°*x 

Hours  and 
Minutes. 

?SJ5 

'£ 

Is 

^  a  ct 

i 

—  ~u 

rt^J 

X 

u 

S 

j 

£ 

n 

iSg? 

7191 

July  2 

5.00  A.M. 

1/4 

23.5 

95 

4-7 

7h.  5im. 

10  693 

21 

7192 

"  2 

6.00 

174 

23-5 

95 

5-2 

8h.  sim. 

12  143 

14 

7195 

"   2 

9.00  " 

174 

23-5 

95 

6.8 

nh.  5im. 

16293 

48 

Agitated  surface  of  sand  layer 

7196 

"   2 

9.51   " 

174 

23-5 

95 

I2h.  4om. 

17443 

38 

at  9.39  A.M. 

7197 

"   2 

11.30  " 

174 

23-5 

95 

'5.8 

14(1.  igm. 

19763 

31 

7198 

"   2 

I.I7  P.M. 

175 

23.5 

95 

oh.  o6m. 

'55 

73 

7199 

"   2 

2.OO   " 

175 

23.5 

95 

2-7 

oh.  4gm. 

205 

24 

7202 

"   2 

3.30   " 

175 

23.5 

95 

3-o 

2h.  igm. 

3335 

26 

7215 

"   2 

5.00   " 

175 

23-5 

95 

4-1 

3h.  49m. 

5425 

27 

7216 

"   2 

8.00  " 

175 

23-5 

95 

4-9 

6h.  4gm. 

9635 

25 

7218 

"   2 

10.55  " 

176 

23-5 

95 

oh.  0501. 

145 

58 

7219 

"   2 

II.  OO   " 

176 

23-5 

95 

2.1 

oh.  torn. 

300 

48 

7221 

"   2 

11.30  " 

176 

23.5 

95 

2.2 

oh.  4om. 

965 

51 

7222 

"   2 

12.30  A.M. 

176 

23-5 

95 

2-5 

ih.  4om. 

2  505 

57 

7223 

"   2 

1.30   " 

176 

23.5 

95 

2-7 

2h.  4Om. 

3775 

33 

7224 

"   2 

2.30   " 

176 

23.5 

95 

3-1 

3h.  4om. 

5  175 

41 

7226 

"   2 

3.30   " 

176 

23.5 

95 

3-4 

4h.  40m. 

6595 

45 

7227 

"   2 

5-00   " 

176 

23-5 

95 

4.0 

6h.  lom. 

8715 

49 

7228 

"   2 

8.00  " 

176 

23-5 

95 

5-3 

gh.  lom. 

12  825 

67 

7230 

"   2 

g.oo  " 

176 

23-5 

95 

5-8 

loh.  lom. 

14225 

86 

7231 

"   2 

o.oo  " 

176 

23-5 

95 

6.4 

nh.  lom. 

15635 

88 

7232 

"   2 

I.OO   " 

176 

23-5 

95 

6.7 

I2h.  lom. 

17035 

94 

7233 

''   2 

2.OO  M. 

176 

23.0 

93 

72 

I3h.  lom. 

18435 

73 

Closed  outlet  at  12.00  M. 

72433 

"   2 

1.  08  P.M. 

179 

23.5 

95 

oh.  o6m. 

'55 

170 

7244 

"   2 

I.  12   " 

179 

23.5 

95 

oh.  lom. 

255 

162 

7245 

"   2 

1.24  " 

179 

23-5 

95 

oh.  22m. 

505 

134 

7247 

"   2 

1-45  ' 

179 

23.5 

95 

oh.  43m. 

i  001; 

107 

Closed  outlet  at  11.45  ['-M- 

7248 

"   23 

2.51  A.M. 

1  80 

23-5 

95 

oh.  o6m. 

148 

in 

7249 

"   23 

2.56  " 

1  80 

23-5 

95 

oh.  nm. 

248 

152 

7251 

"  23 

1.30  " 

i  So 

23-5 

95 

2.2 

oh.  45m. 

i  048 

Sg 

7252 

"  23 

2.30  " 

180 

23.5 

95 

2.5 

ih.  45m. 

2438 

61 

7254 

'  23 

4.00  " 

1  80 

23.5 

95 

2-7 

3h.  ism. 

4638 

68 

7255 

"  23 

5.30  " 

1  80 

23.5 

95 

3-5 

4h.  45m. 

6808 

77 

7265 

'  23 

8.24  P.M. 

182 

23-5 

95 

oh.  o6m. 

150 

283 

7266 

'  23 

8.28   " 

182 

23-5 

95 

oh.  lom. 

250 

273 

7267 

"  23 

8-39   " 

182 

23-5 

95 

oh.  2im. 

500 

136 

7271 

"  23 

g.oo  " 

182 

23-5 

95 

oh.  42m. 

I  OOO 

188 

Closed  outlet  at  9.00  P.M. 

7272 

1  23 

0.18  " 

183 

23-5 

95 

oh.  lom. 

144 

223 

7273 

"  23 

0.22   " 

183 

23-5 

95 

oh.  1401. 

244 

258 

7274 

"   23 

0.33  " 

183 

23.5 

95 

oh.  25m. 

494 

275 

7275 

"  23 

I.OO   " 

183 

23-5 

95 

2-3 

oh.  52m. 

I  164 

231 

7277 

'  23 

2.OO   " 

183 

23-5 

95 

2-4 

ih.  52m. 

2  554 

193 

7278 

'  24 

I.OO  A  M. 

183 

23-5 

95 

2-7 

2h.  52m. 

4054 

119 

. 

7279 

'  24 

2.OO   " 

183 

23.5 

95 

2.8 

3h.  52m. 

5454 

82 

Closed  outlet  at  2.00  A.M. 

7281 

'  24 

3-05   " 

184 

23-5 

95 

oh.  osm. 

'47 

208 

7282 

"  24 

3.09   " 

184 

23-5 

95 

oh.  ogm. 

247 

200 

7283 

"  24 

3.20   " 

184 

23-5 

95 

oh.  2om. 

497 

138 

7285 

"  24 

3-45   ' 

184 

23-5 

95 

oh.  45m. 

I  067 

92 

Closed  outlet  at  3.45  A.M. 

7286 

"   24 

4.50   " 

185 

23-5 

95 

oh.  o6m. 

146 

IO2 

7287 

"  24 

4-54   ' 

185 

23-5 

95 

oh.  lom. 

246 

126 

7289 

'  24 

5.30   " 

185 

23-5 

95 

2.2 

oh.  46m. 

I  096 

91 

7290 

'  24 

6.1X3   " 

185 

23-5 

95 

2.5 

ih.  i6m. 

i  836 

82 

7291 

"  24 

8.00  " 

185 

23-5 

95 

2.8 

3h.  l6m. 

4696 

133 

7293 

'  24 

g.oo  " 

185 

23-5 

95 

3-o 

4h.  i6m. 

6  116 

I67 

7294 

'  24 

10.00  " 

185 

23-5 

95 

3-2 

5h.  l6m. 

7  546 

253 

Closed  outlet  at  10.02  A.M 

RESULTS    OF    BACTERIAL   ANALYSES— WITH    PERSULPHATE   OF    IRON. 


1897 

5271 

April  6 

3.30  A.M. 

'  4 

23-5 

95 

3-3 

oh.  43m. 

i  ug 

141 

5272 

"       6 

4-30     "                    4 

23-5 

95 

4.0 

ih.  43m. 

2469 

192 

5273 

6 

5.30     " 

4 

23-5 

95 

5-8 

2h.  43m.      3  755 

89 

5275 

6 

10.30     " 

5 

23-5 

95 

4.0 

2h.  osm. 

2  760 

247 

36° 


WATER   PURIFICATION  AT  LOUISVILLE. 


RESULTS    OF    BACTERIAL    ANALYSES— WITH    PERSULPHATE    OF    IRON.— Continued. 


Rat 

eof 

u 

S 

C 

ollected. 

Filtr, 

tion. 

£ 

il 

~ 

• 

U 

in  u 

Period  of 

V.    &* 

a 

<u 

Number 

6. 

0  0. 

•n 

ServiceSince 

ii  —  J 

^   V-' 

a 

Run. 

£  u 

O  u  5 

S3 

Last 
Washing. 
Hours  and 

IK 

Q 

Remarks. 

"3 

*  Date. 

Hour. 

o  a 

|^S 

"3 

Minutes. 

Sil 

'si 

'0 

"2  S 

~  a.  3" 

1 

"i-<  U 

n  U 

w 

u 

S 

E 

n 

1897 

5276 

April    6 

-  o   oo   M 

f 

23  •  5 

95 

840 

5277 

6 

2.00    P.M. 

6 

23.5 

95 

3.1 

ih.  i8m. 

1  714 

igi 

5278 

"       6 

3.00       " 

6 

23-5 

95 

5-6 

2h.  i8m. 

3  '54 

172 

5280 

6 

3-30        " 

6 

23-5 

95 

7-7 

2h.  4801. 

3814 

172 

Closed  outlet  at  3.42  P.M. 

5281 

6 

5.OO        " 

7 

23o 

95 

3-1 

ih.  oom. 

i  382 

228 

5283 

6 

5.30        " 

7 

23   5 

95 

3-7 

ih.  3om. 

2082 

319 

5293 

7 

10.00  A.M. 

10 

23-5 

95 

5-2 

2h.  oom. 

2837 

168 

5294 

7 

IO.3O       " 

IO 

23-5 

95 

7-5 

2h.  3001. 

3517 

177 

Agitated  surface  of  sand  layer  at 

5295 

7 

10.37       " 

10 

23-5 

95 

2h.  35m. 

3617 

397 

10.32  A.M. 

5296 

7 

10.40       " 

10 

23-5 

95 

2h.  38m. 

3688 

415 

5297 

7 

10.43       " 

IO 

23.5 

95 

2h.  4im. 

3756 

239 

5298 

10.46       " 

IO 

23-5 

95 

2h.  44111. 

3824 

198 

5299 

7 

10.49      " 

10 

23-5 

95 

2h.  47m. 

3892 

182 

5300 

7 

10.52      " 

10 

23-5 

95 

2h.  5om. 

3963 

159 

5301 

7 

10.55      ' 

IO 

23-5 

95 

.... 

2h.  53m. 

4035 

177 

5302 

7 

11.30     " 

10 

23-5 

95 

5-2 

3h.  28m. 

49'7 

1  66 

5303 

7 

1.  00    P.M. 

10 

23-5 

95 

6.6 

4h.  58m. 

7027 

M5 

5304 

7 

2.00       " 

IO 

23-5 

95 

5h.  58m. 

8472 

142 

5305 

7 

2.O6       " 

10 

23-5 

95 

6h.  oim. 

8540 

260 

5306 

7 

2.Og 

10 

23-5 

95 

6h.  04m. 

8612 

810 

5307 

7 

2.12       " 

IO 

23-5 

95 

6h.  o7m. 

8679 

211 

5308 

7 

2.15       " 

10 

23-5 

95 

Gh.  lorn. 

8749 

1  69 

5309 

"       7 

2.18       ' 

IO 

23-5 

95 

6h.  I3m. 

8817 

126 

7 

2.21       " 

IO 

23-5 

95 

6h.  i6m. 

8887 

141 

[4-48  P.M. 

5311 

7 

3.00       " 

IO 

23-5 

95 

7.0 

6h.  55m. 

9  747 

1  60 

Agitated  surface  of  sand  layer  at 

5313 

7 

4-50       " 

10 

23-5 

95 

7-9 

8h.  42in. 

12  117 

181 

Closed  outlet  at  5.00  P.M. 

5338 

9 

3-3"       " 

14 

23-5 

95 

3-5 

oh.  35m. 

836 

137 

5340 

9 

5.00     " 

14 

23-5 

95 

6.2 

2h.  05m 

2848 

28g 

5341 

9 

5.25       ' 

14 

23.5 

95 

6.8 

2h.  3om. 

3278 

187 

5342 

9 

IO.3O  A.M. 

14 

23-5 

95 

6.0 

5h.  49111. 

6862 

232 

5344 

9 

I2.OO  M. 

14 

23-5 

95 

6.5 

6h.  1  5m. 

8643 

39° 

1       12 

7.30   P.M. 

18 

23-0 

93 

4-5 

2h.  05m. 

3093 

I  375 

5382 

"       12 

8.30       " 

18 

23.5 

95 

5-1 

3h.  osm. 

4413 

191 

5334 

"       12 

9-30       " 

18 

23-5 

95 

5-9 

4h.  osm. 

5922 

88 

5385 

"       12 

10.30       " 

18 

23.5 

95 

6.6 

5h.  osm. 

6813 

1  20 

5386 

"        12 

11.30       " 

18 

23.5 

95 

6.9 

5h.  4im. 

7983 

195 

5387 

"       13 

12.30  A.M. 

18 

23-5 

95 

7-7 

6h.  4im. 

9413 

183 

Agitated  surface  of  sand  layer  at 

5388 

'      13 

1.30      " 

18 

23-5 

95 

6.5 

7h.  3om. 

10693 

IOO 

12.53  A.M. 

5389 

'      13 

2.30      " 

18 

23-5 

95 

6-7 

8h.  35m. 

12043 

470 

5391 

'      13 

3.21       ' 

18 

23-5 

95 

gh.  23m. 

13  123 

425 

Agitated  surface  of  sand  layer  at 

5392 

'      13 

3-24      ' 

18 

23.5 

95 

gh.  26m. 

13  193 

gio 

3.18  A.M. 

5393 

'     13 

3-27      " 

18 

23-5 

95 

gh.  2gm. 

13273 

256 

5394 

"      13 

3.30      " 

18 

23-5 

95 

7-7 

gh.  32m. 

13353 

202 

[4.12  A.M.  and  4.59  A.M. 

5395 

'     13 

4-3°      " 

18 

23-5 

95 

7-9 

I  oh.  30111. 

14653 

147 

Agitated  surface  of  sand  layer  at 

'     13 

5.30      " 

18 

23-5 

95 

nh.  27m. 

15853 

287 

Closed  outlet  at  5.46  A.M. 

5425 

'     M 

10.30   P.M. 

25 

23-5 

95 

2-5 

oh.  3om. 

665 

ig2 

5426 

'     M 

11.30      " 

25 

23-5 

95 

4.0 

ih.  3om. 

2075 

310 

5427 

'      15 

12.30  A.M. 

25 

23-5 

95 

4-4 

2h.  30111. 

3475 

120 

5428 

'      15 

1.30      " 

25 

23-5 

95 

4.8 

3h.  30111. 

4865 

47 

5429 

'     15 

2.30      " 

25 

23-5 

95 

5-5 

4h.  3om. 

6255 

78 

5431 

'     15 

3-30      " 

25 

23-5 

95 

6.8 

5h.  3om. 

7645 

7 

5432 

'     15 

4.30      " 

25 

23-5 

95 

7-o 

Gh.  3om. 

9035 

6g 

Agitated  surface  of  sand  layer  at 

5433 

"     15 

5.30      " 

25 

23-5 

95 

7.8 

7h.  25m. 

10305 

264 

4-37  A.M. 

5451 

"     16 

g.oo     " 

31 

23-5 

95 

3-0 

ih.  oom. 

I  392 

58 

5452 

"     16 

10.  OO       " 

31 

23-5 

95 

3-5 

2h.  oom. 

2  782 

98 

5453 

"      16 

1  1  .  OO      " 

31 

23-5 

95 

4.0 

3h.  oom. 

4  182 

T59 

5454 

"     16 

12.  OO  M. 

31 

23-5 

95 

4-4 

3h.  35m. 

4932 

ng 

5455 

"     16 

1.  00   P.M. 

31 

23-5 

95 

5-0 

4h.  35m- 

6  322 

239 

5459 

"      16 

2.00       " 

31 

23-5 

95 

5-7 

5h.  35111. 

7  732 

310 

Closed  outlet  at  2.13  P.M. 

5489 

"       21 

8.00     " 

35 

23-5 

95 

3-9 

ih.  23m. 

2135 

183 

5491 

"      21 

10.30     " 

35 

23.0 

93 

4-5 

3h.  26m. 

4775 

71 

5492 

"       21 

11.30    " 

35 

23.0 

93 

5-o 

4h.  26m. 

5  635 

log 

5493 

"       22 

12.30  A.M. 

35 

23-5 

95 

6.4 

5h.  26m. 

7425 

Go 

5494 

"      22 

1.30     " 

35 

23-5 

95 

8.0 

6h.  26m. 

8775 

114 

INVESTIGATIONS  OF  THE   WATER  COMPANY  FROM  APRIL   TO  JULY,  1M7.  361 


RESULTS    OF    BACTERIAL    ANALYSES— WITH    PERSULPHATE    OF 


Collected. 

K;iti      : 
Filtration. 

1 

1 

15 

1 

Number 

6 

!& 

•c 

Period  of 
Service  Since 

s|L- 

u  u- 

8 
y. 

Run. 

v    . 

fc  3 

151 

I 

Washing. 

Hours  and 

ll£ 

£.5 

g 

Remarks. 

Date. 

Hour. 

§^K 

o 

Minutes. 

ii  %  & 

t  £ 

•c 

11 

3&JT 

i 

%2>£> 

iju 

in 

<_> 

H 

j 

(L, 

00 

1897 

5496 

April  22 

3.00  A.M. 

35 

23.0 

93      S.8    yh.  56111. 

10  805 

II?  Agitated  surface  of  sand  layer  al 

5497         "      22 

4.00       " 

35 

23.5 

95      8.o;  8h.  5401. 

12  115 

495       3.02A.M. 

5605         "      29 

7.00    I'.M. 

51 

23.5      95      2.7|  oh.  i6m.           384 

45! 

5606,        "      29 

9.00     " 

51 

23-5      95      3-9    2h.  i6m.        3  174 

43 

5607        "      29 

IO.OO 

51 

23-5      95      4-i 

3!).  1  6m. 

4564 

29' 

5609 

"      29 

11.00       " 

5i 

23-5      95 

5-6 

4h.  i6m. 

5924 

47 

5610 

'      29 

12.00       " 

5i 

23-5 

95 

6.4 

5h.  i6m. 

7304 

32 

5611 

"      3° 

I.OO  A.M. 

51 

23-5 

95 

8-3 

6h.  i6m. 

8694 

44  Agitated  surface  of  sand  layer  at 

5612 

"      30 

2.OO       " 

51 

23-5 

95 

5-8 

7h.  iim. 

gg64 

29      i  .  1  9  A  .  M  . 

5614 

"      3° 

3.00       " 

5i 

23-5 

95 

8.0 

Sh.  Tim. 

ii  3M 

28 

=  !,,= 

"     3" 

3-5<)     " 

5' 

23.0 

93 

8.8 

gh.  o6m. 

12  544 

19 

56l6 

"     30 

4.07     ' 

51 

23.5 

95 

8.0 

9h.  O9m. 

12  624 

47 

=  ''17 

"     3° 

4.10     " 

51 

23-5 

95 

8.1 

oh.  1  2m. 

12674 

28 

5618 

"     30 

4.13     " 

5i 

23-5 

95       8.2 

()h.  15111.      12  734 

1  1 

5619 

••     30 

4.16     " 

5i 

23.5 

95      8.3 

9h.  iSm.      12  814 

16 

562o|         '      30 

4.30     " 

51 

21.0        89        9.3 

gh.  32m.      13  144 

33  Closed  outlet  at  4.49  A.M. 

6976    July    o 

12.  l8    I'.M.                      154 

23-5 

95 

oh.  o6m.           150 

'99, 

6977       "       o 

12.26       "                         154 

230 

95 

oh.  14111. 

342 

186  Closed  outlet  at  12.26  P.M. 

6978         '       o 

2.15       " 

155 

23.5 

95 

oh.  07111. 

167 

97 

6980       "       o 

2.3O       " 

155 

23-5 

95         2.2 

oh.  22m. 

497 

"4 

6982        "       o 

2.45     " 

155 

23.5 

95     

oh.  37m. 

807 

7"| 

6983        '  '       o 

3.00     " 

155 

23.5 

95 

oh.  52m. 

I  187 

541 

6984       ''       o 

4.1x5      "                    155 

23.5 

95      3-5 

ih.  52m. 

2  537 

58  Closed  outlet  at  4.04  P.M. 

RESULTS    OF    BACTERIAL    AN  ALYSES—  WITH    COPPERAS. 

1897 

6720  June  28 

12.50  A.M.                         23 

23-5      95 

oh.  o6m. 

141 

6721        "     28 

12-55       ' 

23 

23-5      95 

oh.  nm. 

251 

6722       "     28 

I  .  OO 

23 

23-5      95 

2.8 

oh.  i6m. 

371 

6723        "     28               I.  10     " 

23 

23-5      95 

oh.  26m. 

581 

6751        "     30 

11.56 

28 

23-5      95 

oh.  o6m. 

154 

34 

6752        "     30 

12.  OO  M. 

28 

23  •  5      95 

2.0 

oh.'  lorn. 

254 

4' 

6756        "     30 

12.30  I'.M. 

28 

24.0      97 

2.6 

oh.  4001. 

964 

121 

6757'       "     3° 

I.OO 

28 

23-0      93 

2-9 

ih.  lorn. 

1644 

170 

6758        "     30 

1.30    "               28 

23.0      93 

3-2 

ih.  40111. 

2324 

229 

6759         '     30 

2.0(>       "                            28 

22.0 

89 

2h.  lorn. 

2934 

147 

Closed  outlet  at  2.00  P.M. 

6761 

"     3" 

4.05       '                              29 

23-5 

95 

2-7 

oh.  ogm. 

220 

254 

6762 

"     3° 

4.30       "                            29 

23-5 

95 

2-7 

oh.  34111. 

800 

188 

6849 

Ju'y  3 

1.40       " 

23-5 

95 

oh.  o7m. 

204 

i  700 

Samples      6849-6857     with     cop 

6853 

3 

2.00       "                            38 

23-5 

95 

3-4 

oh.  27m. 

734 

219 

peras  and  caustic  soda. 

6854 

3 

2.15       '                              38 

23-5 

95 

oh.  42m. 

I  074 

"3 

Closed  outlet  at  2.16  P.M. 

6855 

3 

3-30     "                     39 

23.5 

95 

2.8     Oh.    22111. 

577 

o 

6856 

3 

4.00     "                     39 

23-5 

95 

2.9    oh.  5201. 

I  247 

12 

6857 

3 

4-3°     "                     39 

23-5 

95      2.g:   ih.  22m. 

i  847 

IOi 

RESULTS    OF    BACTERIAL    ANALYSES—  WITH    ELECTROLYTICALLY    PREPARED    HYDRATE    OF 

ALUMINUM. 

1897 

5406 

April  13 

5.30    P.M. 

20 

23.0 

93      2.5 

oh.  04m. 

no 

325 

5407 

'     13 

8.00     " 

20 

23.5      95      4.0 

2h.  34m. 

4580 

2  III  Closed  outlet  at  S.oS  P.M. 

5409 

'     14 

I.OO  A.M. 

21 

23-5      95      4-2 

ih.  nm. 

i  599 

670^ 

5410 

'     M 

2.00       " 

21 

23-5      95      5-8 

2h.  nm. 

2959 

I  100  Closed  outlet  at  2.10  A.M. 

5411 

'      M 

3.00       " 

22 

23-5 

95 

2-9 

oh.  23m. 

521 

369 

5413 

'      M 

4.00       " 

22 

23-5 

95 

4-7 

ih.  23m. 

ign 

236 

54M 

'      14 

5.OO       " 

22 

23-5      95      5-8 

2h.  23m. 

32gi 

i  290 

Closed  outlet  at  5.  10  A.M. 

5415 

'      14 

6.00     " 

23 

22.  ( 

89 

3-1 

oh.  27m. 

6i<] 

387 

55ic 

"       22 

8.30   P.M. 

37 

23-5 

95 

I-' 

2h.  2om. 

3  '35 

242 

Closed  outlet  at  8.32  P.M. 

55" 

"      22 

9-30       " 

38 

23-S 

95 

3-5 

oh.  3om. 

721 

i  125 

5513 

"      22 

I0.3O       " 

38 

23-5 

95 

3-3 

ih.  3om. 

2  III 

99 

55M 

"       22 

11.30       " 

38 

23-  = 

95 

S-r 

2h.  3om. 

35" 

173 

55i? 

"       23 

I.3O  A.M. 

39 

23-! 

95 

2-7 

oh.  48m. 

I  122 

"7 

Closed  outlet  at  1.35  A  M. 

362 


WATER   PURIFICATION   AT  LOUISVILLE. 


RESULTS    OF    BACTERIAL   ANALYSES— WITH    ELECTROLYTICALLY    PREPARED    HYDRATE   OF 

ALUMIN  UM.— Continue  J. 


Rate  of 

J 

.- 

Collected. 

Filtration. 

J! 
u. 

5i 

•J 

.o 

her       SL         jjS._ 

~o 

Period  of 

s.s  • 

O 

Nun 

a 

of 
Ru 

V 

Washing 

0-& 

8.5 

Remarks. 

7, 

Hours  and 

Dale. 

Hour. 

o  i       o  J.3C 

0 

Minutes. 

£  s'£ 

£  = 

•c 

•§S      =  0.0 

o 

-  23 

S;j 

M 

U          S 

" 

u. 

« 

1897 

5517  April  23 

4.30A.M.                 4( 

)        j   23.5       95 

3.0    oh.  56m.        I  325 

217 

5518        "      23 

5-3*^      ''                    4* 

OT       C             flK 

4.2     ill.  58m.        2  085 

5520        "      23 

10.30     "                  41        '  23.5      95 

2.8    oh.  50111.        i  157 

142 

5521         "      23 

11.30      "                    4 

23-5      95 

3.  7    ih.  5om. 

2557 

148 

5522         "      23 

12.30  P.M.                 41           23.5       95 

4.8:   2h.  50111. 

3917 

107 

5523        "      23 

1-3°     "                   41           23.5  .    95 

7.5    3h.  50111. 

5  257 

179 

Closed  outlet  at  1.45  P.M. 

5544        "      26 

9.30A.M.                 44           23.5       95 

3.3!    ih.  14111. 

i  722 

380 

5545         "      26 

10.30      "                    4 

1          24.0      97 

4.2      2ll.    O2I11. 

2  852 

254 

5546         '     26 

1  1  •  30      "                    4 

4          23.5      95 

6.  5    3h.  02111. 

4232 

247 

5547         '     26 

12.30  P.M.                 44           23.5       95 

8.7!   4h.  oam. 

5  602 

232 

Agitated  surface  of  sand  layer  at 

5548        "     26               1.30     "                   44          23.5      95 

0.9    5h.  oom. 

6  962 

485 

12.40  P.M. 

5550         '     26 

5.30      "                    4 

>          23.5      95 

2.7    2h.  2IH1. 

2798 

145 

5551        ''     26              6.30     "                   4 

)          23.5      95 

3.0    3h.  21111. 

4  288 

595 

5552        '1     26              7.30     '1                   45        ,   23.5      95 

4.9    4li.  2irn. 

5  608 
6  838 

400 

5553        "     26 
5554        "     26 

"•J'J                                     4 

9-30     "                   4 

)                -JO         V  3 

)           23.5       95 

7-5    5^  •  2  1  in. 
5.3    Oh     Kjm. 

8  168 

233 

07 

9.04  P.M. 

5559        "     26 

10.30     "                   4 

>           23.5       93 

S.o    7)1.  igm. 

9538 

141 

Closed  outlet  at  10.35  P.M. 

5571        "     28 

9.00  A.M.                 4 

3           24.0      97 

7.2    2h.  56m. 

4093 

169 

Agitated  surface  of  sand  layer  at 

5572        "     28 

10.00     "                   48          24.0      97 

4.5    3h.  56m. 

5423 

201 

9.44  A.M. 

5573        "     28 

i  i.oo     "                  4 

3          23.5      95 

6.2    4h.  54111. 

6930 

435 

5577         '     28 

12.00       "                         4 

3          23.5      95 

7.0    5h.  54111. 

8  320 

455 

5578        "     28 

i.oo  P.M.                4 

5       '   23.0      93 

7.6    6h.  54m.       9680 

995 

5583        "     28 

4.00     "                  4 

)          23.0      93 

2.6    oh.  32m.           598 

237 

5584         '     28 

5-3')     "                  4 

)          23.5      95 

3.O     2ll.   02111.          2  678 

199 

5585        "     28 

8.3'->     "                   49       !   23.5      95 

6.4    5h.  02m.       6868 

319 

[9.52  P.M. 

5587        "     28 

9-3»     "                   49          23.5      95 

S.o   6h.  oam.       8  228 

453 

Agitated  surface  of  sand  layer  at 

5588         '     28 

10.30      "                    49           23.5       95 

4.8    6h.  59m. 

8848 

585 

Closed  outlet  at  10.43  P'M. 

5622        "     30 

9.30  A.M.                 5 

2          23.5      95 

2.4    oh.  0501. 

147 

n5 

5623         '     30 

10.30     "                   5 

2          23.5      95 

3.0    ih.  05111. 

i  557 

no 

5624        '30            11.30     "                  5 

2          23.5      95 

4.8    2h.  osm.        2957 

177 

5625        "     30            12.30  P.M.                5 

2          23.5      95 

5-3    3h.  05111.       4357 

47 

[2.06  P.M. 

5626        "     30 

1.30     "                   5 

2          23.5      95 

7.1    4h.  osm. 

5  747 

195 

Agitated  surface  of  sand  layer  at 

5627        "     30              2.30     "                   5 

2          23.5      95 

5.6    5)1.  03m. 

7"47 

253 

[4.10  P.M. 

5632        "     30              4.00     "                   5 

2          23.5      95 

7.7!  oh.  33m.       9  087 

410 

Agitated  surface  of  sand  layer  at 

5633        "     30              5.00     "                   5 

2          23.5      95 

7.9    "h.  31111.      10  297 

333 

Agit.surf.of  sand  layer  at$.O4P.M. 

5634        "     30              5.30     "                   5 

2          23.0      93 

8.0 

7h.  59111.     n  067 

429 

Closed  outlet  at  5.44  P.M. 

5635 

"      30 

S.oo     "                   5 

3          23.5      95 

2.4 

oh.  3im.          698 

141 

5640 

"      30 

9.00     "                   53          23.5      95 

3.0     ill.   31111.         2  258]       158 

5"4i 

'      30 

10.00     "                   53          23.5      95 

4-1 

2h.  3im.        3  538        95 

5642 

'     3" 

11.00     "                   5 

3          23.5,     95 

5-7 

3h.  31111. 

4  908 

90 

5643 

"     30 

12.00     "                   53       :   23.5      95 

S.I 

4h.  24111. 

6248 

83 

Agitated  surface  of  sand  layer  at 

5644 

May 

I.OO  A.M.                      5 

3          23.5      95 

6.  3 

5h.  24111. 

7478 

87 

12.17  A.M. 

5645 

" 

2.00     "                 5 

3          23.5      95 

7-3 

Oh.  24111. 

8818 

164 

5646 

''             i         3  ..oo     "                  5 

3          23.5      95 

7h.  I9m. 

0088 

321 

Agitated  surface  of  sand  layer  at 

5648 

4.00     "                   5 

3          23.5      95 

7-2 

8h.  igm. 

1568 

143 

12.55  A.M. 

5649 

5.00      "                    5 

3          23.5      95 

9h.  I4m. 

2678 

429 

Agitated  surface  of  sand  layer  at 

5650 

5.03     "                   5 

3          23.0      93 

9!].  1  7m. 

2  768 

243 

4.55  A.M. 

5651 

" 

5-of)     "                   5 

3          23.5      95 

9h.  2om. 

2838 

179 

5653 

" 

9.00     "                   5 

4          23.5      95 

2.8 

oh.  45m. 

I  031 

121 

5654 

" 

10.00     "                   5 

4          23.5      95 

3-2 

ih.  45m. 

2441 

93 

5055 

" 

11.00     "                  5 

4-          23.5      95 

3-5 

2h.  45m. 

3SSl 

95 

5656 

" 

12.  OO       "                         5 

t          23.5      95 

3.8 

3h.  45m. 

5  251 

92 

5657 

"                               I.OO  P.M.                      5 

4          23.0      93 

5-0 

4h.  45m. 

6  601 

IOO 

5658 

2.00     "                   5 

^          23.5      95 

6.0 

5h.  45m. 

7981 

69 

5663 

3.0°     "                  5 

\          23.5      95 

7-7 

6h.  42m. 

93Si 

121 

Agitated  surface  of  sand  layer  at 

5738 

"       7 

I.OO  A.M.                      5 

i          23.5      95 

4-5 

ih.  iSm. 

i  528 

130 

3.08   P.M. 

5739 

7 

4.30     "                 5 

>          23.5      95 

2.5 

oh.  23m. 

611 

114 

-   Oi 

5744 

7 

5.00     "                  5 

'          23.5      95 

2.6 

oh.  53111. 

I  331 

I2g 

5745 

7 

6.00     "                   5 

>          23.5      95 

4-4 

ih.  53m. 

2  761 

92 

5746 

7 

9.30     "                   5 

7          23.5      95 

2.7 

oh.  28m. 

577 

252 

5751 

7 

10.30     "                   5 

7          23.5      95 

3-1 

ih.  28m. 

1947 

214 

INVESTIGATIONS  OF  THE   WATER  COMPANY  FROM  APRIL   TO  JULY,  1897.  363 


RESULTS    OF    BACTERIAL   ANALYSES— WITH     ELECTROLYTICALLY    PREPARED     HYDRATE    OF 

ALUMINA.— Concluded. 


Collected. 

Rate  of 

Filtration. 

i 

0 

'S 

i 

Number 

R     I  k  .  •= 

Period  of 
Service  Sine 

5  =  . 

3 

U  j 

e 

a 
7. 

1 

Date. 

Hour. 

of 
Run. 

U.    g             -  .?     -            — 

Was'hmif. 
H-.urs  and 
Minutes. 

ii 

A  & 

Remarks. 

•3 

"5  «£        ~  D.  n      .  c 

U         S.            _; 

£ 

1° 

1897 

5752 

May    7 

11.30  A.M. 

57 

23-5       95       4-1 

2h.  28m 

3287 

319 

5753 

7 

12.30   P.M. 

57        23.5      95      5-5      3"-  2Sm 

4  537 

28g    Closed  outlet  at  12.33  ''-M- 

5754 

7 

2.30     " 

58     '   23.5      gs      2.2      oh.  I7m 

3<)7 

5755 

7 

3.30    " 

58        23.5      95      3.2      ih.  17111 

i  797       139 

5760 

7 

4.30    " 

58        23.5      g5      4.7      2h.  I7m 

3  187  i      175 

6806 

July    2 

4.45  A.M. 

133        23.5      95     .... 

oh.  o6m. 

150       170  • 

6807 

2 

4-50     " 

133 

23.5       95     

oh.  nm. 

250         89 

6808 

"          2 

5.00     " 

133 

23.5      95      2.  i      oh.  2im 

480 

136 

68og 

"         2 

5.30   " 

133 

23.5      95      2.2      oh.  5im. 

i  170 

60 

6810 

"          2 

6.00     " 

133 

23-5      95 

2.3      ih.  2im. 

i  830 

52 

6815 

"         2 

g.oo     " 

133 

23.0      93 

4.0      4h.  1301. 

5830 

127 

6816 

"          2 

10.30     " 

134 

23-5      95 

2.2i     oh.  ogm. 

214 

112 

6817             "          2 

11.30   ••           134 

23-5      95 

2.7      ih.  ogm.     i  594         73 

6821             "          2 

1.  00    P.M.                   134 

23-5      95 

3.3      2h.  39111.     3  704       126 

6823             "          2 

3-53     "                 135     !   23.5      95 

oh.  13111.        311  !      147 

Closed  outlet  at  3.53  P.M. 

RESULTS  OF  BACTERIAL  ANALYSES—  WITH   ELECTROLYTICA1.LY   PREPARED  HYDRATE  OF  IRON. 

I8g7 

| 

5346 

Apri    ii 

3.00  A.M. 

15 

23.0'     93      2.8      oh.  50111.      i  153     4000! 

5347 

"      ii 

4.30  P.M.               15 

23-0,     93      3.9      2h.  20111.     3123     5410 

5350 

"      ii 

5.30       " 

15 

23.0      93      4.2      3h.  20111.     4403     7900 

5351 

"      1  1 

6.3O       " 

15 

23-0'     93   !   5.0      4h.  2om.      5723     6000 

5352 

"      ii 

7.30       " 

15          24.0      97      6.0      5h.  20111.      7  123     9800 

5353 

"      ii 

8.30       " 

15 

22.  o      8g      7.3      6h.  2om.|    8353   24000 

5355 

"      ii 

9-3°     " 

15 

22.0      89      S.o      7h.  igm. 

9663  21  ooo  Agitated  surface   of  sand   layer 

5356 

"      n 

9-43     " 

15          23.5;     95 

6.6 

7h.  32111. 

10  073     6  650!     at  9.37  I'-M. 

5357 

"      ii                9.46     " 

15          23.5 

95 

7h.  35m. 

10143  44500 

5359 

"      "                 9-49     " 

15          23.5      95 

7h.  3Sm. 

10203  10000 

5360 

'     ii 

9.52     " 

15          23.5      95      7-i:     7h-  4im- 

10  263'  12  COO 

5364 

"      ii 

11.30     " 

16          18.0      73 

2.0      oh.  38m. 

662       2  72O 

5365 

"       12 

I2.3O  A.M. 

16 

18.0 

73 

2.7,     ih.  38m. 

I  712 

2  goo 

5366 

"         2 

1.30       " 

16 

18.0 

73      3.2      2h.  38m. 

2  772 

i  680 

5367 

2                2.30     "                 16 

18.0 

73 

4.0      3h.  38m. 

3  ,M)2 

2  2OO 

5369 

2                3.30     "                 16          17.0 

6g 

5.0      4)1.  38m. 

4842       2350 

5370 

2                      5.00       " 

17 

18.0 

73 

2.  i      oh.  som. 

892       I  600 

5371 

"          2                      6.OO       " 

17 

18.0 

73 

3-0 

ih.  5om. 

I  gg2 

2030 

5373 

"       2                g.oo     " 

17 

17-5 

71 

5-0 

4h.  som. 

4g32   15  200 

5374 

"          2                    IO.OO       " 

17          16.0 

65 

5-9 

5h.  som. 

5  go2   12  600 

5375 

"          2                    II.  OO       " 

17 

18.5 

75 

7.0 

6h.  som. 

6  882   13  500 

5376 

"          2 

12.00      M. 

17 

14.0 

57 

6.0 

7h.  5om. 

7882 

12  700 

5377 

'          2                      1.  00  P.M. 

17 

18.0 

73 

7-o 

8h.  som. 

8782 

4640 

5378 

"          2 

2.00      " 

17 

16.5 

67 

8.0 

gh.  som. 

g  782     6  400 

5379 
5417 

"          2 

"        4 

3.00    " 

1.30      " 

!7 

17.0 

69 

8.2    loh.  soin. 
...          nh     r  c  m  _ 

10  762     9  450 
355        ^7I 

54i8 

4 

5.00     " 

25 

23-5 

95 

3-9 

ih.  05  m. 

i  715 

42g 

5420 

4 

5-30     " 

25 

23.0 

93 

4.0 

ih.  35m. 

2375 

755 

5461 

"       o 

8.30     " 

32 

23-5 

95 

5-8 

3h.  56m. 

5400 

i  240 

5462 

"       o 

9.30     " 

32 

23-5 

95 

7-o 

4h.  56m. 

6776 

i  450 

5468 

"       o 

12.  OO      " 

33 

23-5 

95 

3-0 

ih.  oom. 

I  404 

449 

5469 

1  ' 

1.  00  A.M. 

33 

23-5 

95 

4-2 

2h..ootn. 

2744 

397 

5470 

' 

2.OO      " 

33 

20.  o 

81 

5-9 

3h.  oom. 

3994 

295 

5471 

" 

3.OO      " 

33 

20.  o 

81 

6.8 

4h.  oom.     5  154 

267 

5472a 

4.00      " 

33 

20.  O 

81      7.5'     5h.  oom.     6  324 

347 

5474 

g.oo     " 

34 

18.0 

73      3-5      3h.  25m.     3497 

167 

5475 

' 

10.00       " 

34 

18.0 

73      4.7;     4h.  25m.     4357 

200 

5476 

11 

II.  OO       " 

34 

18.0 

73      5.0      5h-  25m. 

5647 

139 

5477 

'  ' 

12.00      M. 

34 

18.0      73      6.0      6h.  25111. 

6697 

17- 

5478 
5479 
5480 

» 

I.OO    P.M. 
2.OO 
3.00     " 

34 
34 
34 

18.0 
18.0 
18.0 

73 
73 
73 

7.o|     7h.  25m. 
5.6|     8h.  25111.; 
7.81     gh.  25111. 

7747 
8777 
9823 

217                                            [at  1.35  I'.M. 
138  Agitated   surface  of  sand  layer 
184  Agitated   surface  of  sand  layer 

5481 

3.06     ' 

34 

18.0 

73 

gh.  3im. 

99'7 

420 

at  3.02  P.M. 

3"4 


WATER   PURIFICATION   A  7'  LOUISV/LLh. 


RESULTS    OF    BACTERIAL    ANALYSES— WITH    ELECTROLYTICALLY    PREPARED    HYDRATE 

OF    IRON.  —  Continue,/. 


1 

Rate  of 

£                             ^ 

Collected. 

Filtration. 

£ 

.5 

.« 

J 

—  «T- 

1't-riod  of       ^  ti 

•§ 

.0 

Number 

a 

0  0. 

•a 

ServiceSince     w.E  ^ 

u 

E 

3 

R  un 

«j   .      ^  :-  '£•    ^ 

W  'shine        £  "£ 

~  *J 

Remarks 

^ 

[i.  "            *•  r       ~ 

Hours  and      -c^u 

.-•- 

Date. 

Hour. 

u  i       o  ,_  I 

o 

Minutes.     ,    tyiS 

£  = 

~ 

'fi      =  0.? 

I 

^25 

5<J 

y> 

<j        2           >J                            fc 

B 

jSg? 

5482 

April  21                 3.09  I'.M. 

34           iS.o      73   .  gh.  34m.     9967 

212 

5483 

"     21                 3.12     " 

34          iS.o      73     ,     gh.  37m.    10017 

192 

5488 

21                       4.OO       " 

34 

iS.o      73   i   6.8    ioh.  igm.    10867 

232 

Agitated  surface  of  sand  layer  at 

5560 

'•    27            8.30    " 

46 

23-5      95   !   3-3      2h.  29111.      3477 

420 

3-49  i'-M- 

5565 

'       2-                      9.30       " 

46           23.5       95       3-9      3h.  29111.      4807 

740 

5566 

"       20                       I.OO  A.M. 

47           23.5       95       2.8       ih.  oom.      i  347 

248 

5567 

"       28                      2.OO 

47          23.5      95      3-1,     2h.  oom.     2  707 

'79 

5568 

"      28 

3.00      " 

47          23.5      95      4.1       jh.  oom.     4037 

202 

6478 

June  19 

0.05       " 

88 

23.5      95     <)h-  °5"i-         131 

387 

6479 

"      19                o.  I  o     " 

88 

20  .  o      81 

.  .  .  .      on.  lom.         231 

292 

6480 

"      19                0.15      " 

88          20.0      81     oh.  15111.         331 

427 

6481 

"     ig               0.30     " 

88       i   22.0      89 

.  .  .  .       oh.  30111.         661 

237 

6482 

'      19     1           °-45      ' 

88 

34-5      99 

oh.  45m.      i  031 

295 

6483 

"      19                  I.oo      " 

88 

24.5      99 

.  .  .  .       ih.  oom.      I  401 

3O2 

6484 

"      ig                  1.40      " 

89 

10.0      40 

oh.  osm.:         82 

251 

6485 

'      19                  T-45      ' 

89 

10.  0        40 

oh.  lom.         132 

299 

6486 

'19                  1.50      " 

Sg 

12.0         48 

oh.  ism.         192 

249 

6487 

'      19                 '.55      ' 

89 

I2.O         48 

oh.  20111.         252 

26l 

6488 

'       19                      2.00    I'.M. 

Sg 

18.5      75 

oh.  3om.         437 

301 

6489 

"        19 

2.15     ' 

89 

18.5      75 

.  .  .  .      oh.  4om.        622 

235 

6490 

'        19 

2.32     " 

89 

23.0      g3 

....'<     oh.  5701.      i  012 

263 

6491 

'        19                      1.30       " 

Sg 

24.0      97 

i.o      ih.  55m.      2  442 

'97 

6492 

19                      2.30       " 

Sg 

23.5      95 

1.5       2h.  55m.      3  842 

142 

6494 

"       19                      3.3'>       '' 

89 

23-5      95 

1.8      3h.  55m. 

"!  272 

99 

C>495 

'      19 

4.30    " 

Sg 

230      95 

2.0      4h.  55m. 

6662 

260 

6496 

•      19 

5.30   •• 

8g 

23-5      95 

2.1       5h.  55111. 

S  062 

141 

f'497 

'     ig               6.30     " 

8g 

23-5      95 

2.  i(     6h.  55m. 

9352 

154 

6498 

•      19                S.oo     " 

Sg 

23-5      95 

2.3      Sh.  2501. 

II  402 

145 

6500 

"      19                9-30     " 

Sg 

23-5      95 

2.4      gh.  55m. 

13  222 

201 

6501 

'     i  g                0.09     ' 

Sg 

23-5      95 

ioh.  34111. 

14  152 

250 

Agitated  surface  of  sand  layer  at 

6502 

'     19 

O.2I 

Sg 

23-5      95 

6-5 

ioh.  39m. 

14  252 

ig2 

lo.og  r.M. 

6503 

'      19 

i-57     " 

go 

23-5!     95 

oh.  osm. 

71 

342 

6504 

'       20 

2.05    A.M. 

go 

23-5,     95 

2.2 

oh.  13111. 

381 

278 

6505 

"       20 

2.2g       " 

go 

23-5,     95 

oh.  3701. 

Sn 

292 

6506 

•'       20 

1  .  30       " 

go 

23-5      95 

2.6 

ih.  oim.      i  391 

223 

6507 

'       20 

2.OO       " 

do           23.5       95 

2.6 

ih.  jim.j    2  277 

183 

6508 

2O 

4.21     "               gr       '   12.0 

48 

1  .0 

oh.  05m.           fig 

295 

6509 

'       20                    4.26      "                     gl         '    12.0 

48 

i.o      oh.  torn.         129 

377 

6510 

20                 4.30      "                  gl            12.  o      48 

o.g      oh.  14111.         189 

380 

6511 

"       20                      4.45       " 

gl            12.0      48 

oh.  2gm.         359 

281 

6513 

"       20 

5.00       " 

gi           18.5 

75 

1.6 

oh.  44111.        609 

280 

6514 

"       20 

5.30       " 

gl          20.  o 

Si       1.7 

ih.  14111. 

I  229 

274 

6555 

20                6.00     " 

gi           20.  o 

8  1         2.0 

ih    44in.      i  739 

271 

6516 

"       20                      6.30       " 

gl            15.0 

61       1.7 

2h.  1  4m.      2  25g 

205 

6517 

"        2O                        7.  (30        " 

91           15.0 

61       1.7 

2h.  44111.      2  749 

219 

Closed  outlet  at  7.00  A.M. 

6609 

'        24 

12.50       " 

05           23.5 

95     

oh.  O5m.         107 

470 

6610 

'        24 

12.55       " 

05           23.5 

95 

oh.  lom. 

227 

450 

66  1  1 

"      24 

I.OO       " 

05 

23.5 

95 

2-3 

oh.  15111. 

347 

565 

6612 

'    24 

I.  10        " 

05          23.5 

95 

oh.  25m. 

577 

360 

6613 

'    24 

1.20       " 

05           23.5 

9 

oh.  35m. 

807 

268 

6614 

'    24 

1.29       " 

05 

23.5 

9    . 

oh.  44m. 

1047 

385 

Closed  outlet  at  1.29  A.M. 

6616 

'      24 

4.40       " 

06 

20.  o 

8 

oh.  o6m. 

90 

3'5 

6617 

'    24 

4-45       ' 

06 

20.  o 

8 

oh.  nm. 

190 

485 

6618 

'    24 

4.50       " 

06 

20.0 

S 

oh.  1  6m. 

290 

535 

6619 

'    24 

5.00       " 

06 

2O.  O 

8 

i.g 

oh.  26m. 

55° 

390 

6620 

'    24 

5.30       " 

06 

2O.  O 

8 

oh.  56111. 

i  ogo 

435 

6621 

'    24 

6.00     " 

06 

20.0 

S 

2.0 

ih.  26m. 

i  710 

465 

6623 

'    24 

9.00     " 

06 

20.5 

s 

3-o 

4h.  26m. 

5  330 

198 

6624 

'    24 

IO.OO        " 

06 

20.  O 

8 

3-7 

5h.  26111. 

6  480 

258 

6625 

'    24 

I  I.OO       " 

06 

2O.  O 

S 

4-5 

6h.  26m. 

7  820 

229 

6626 

'    24 

I2.OO  M. 

06 

20.0 

8 

4-7 

7h.  26m. 

S  goS 

395 

6627 

'    24 

12.30   P.M. 

06 

19.  o 

77 

4.8 

7h.  5601. 

9480 

475 

Closed  outlet  at  12.30  P.M. 

INVESTIGATIONS  OF  THE  WATER  COMPANY  FROM  APRIL   TO  JULY,  18!>7.  365 


RESULTS   OF    BACTERIAL   ANALYSES— WITH    ELECTROLYT1CALLY    PREPARED    HYDRATE   OF 

IRON  .—Continued. 


Rate  of 

w 

0 

Collected. 

Filtr 

ition. 

£ 

;| 

« 

fc 

X  umber 

I 

o  a 

I'enoa  01 

".s'j 

u  u. 

g 

^ 

—  o    • 

3         „.  L?st 

-a  ~  i) 

v  2i 

Remarks. 

Run 

U   v 

O  o  1 

I         Washmg 

•*  *~  u. 

°"  s 

z 

Date. 

Hour. 

"ol 

c<  ° 

Hours  and 
o         Minutes. 

•: 

^i 

ii 

J! 

•§s 

u 

.-a* 

8 

£ 

n 

1897 

6634 

June  24 

5-45  l'-M. 

os 

iS.o 

73 

1.7      oh.  osm. 

M5 

59° 

6635 

"     24 

7.30      " 

08 

18.0 

73 

2.0      ih.  5001. 

2  065 

625  Closed  outlet  at  7.50  P.M. 

6640 

"     24 

11.55      ' 

10        23.5 

95 

....      oh.  06111. 

IS' 

i  495 

6641 

"     24 

12.00       " 

10        23.5 

95     ....      oh.  nm. 

2Sl 

1680 

6642 

"     25 

12.15  A.M. 

i  > 

23-5 

95   |.  ...      oh.  26m. 

581 

2  750  Closed  outlet  at  12.32  A.M. 

6644 

"      25 

3.12       " 

i        '   18.0 

73     oh.  osm. 

105 

695 

6645 

"    25 

3.20       " 

i       i   18.0 

73 

....       oh.  1301. 

285 

710 

6646 

"      25 

3.30       " 

I             IS.,, 

73 

1.5      oh.  23m. 

485 

545 

6647 

"      25 

4.00       " 

I 

iS.o 

73 

i  .5      oh.  53m. 

I  025 

575 

664s 

"    25 

5.00     " 

I 

iS.o 

73 

1.7       ih.  53171. 

2  065 

260 

6649 

"     25 

6.00     " 

I           I  S  .  o 

73      2.0      2h.  53m. 

3035 

244 

6650 

11       25 

8.00     " 

i           1  8  .  o 

73   ;   2.6      4h.  53m. 

5  275 

1  66 

6652 

"     25 

9.00     " 

i           iS.o 

73      3.0      sh.  47171. 

6445 

152 

6653 

"     25 

10.00      " 

i           18.^ 

73      3-5      f>h.  47m. 

7435 

86 

6654 

"      25 

11.00        " 

i           18.0 

73      4.0      7h.  47m.      8515 

in 

"     25 

12.  OO 

i           18.0 

73      4-5      8h.  47111. 

9625 

131 

6656 

"    25 

I.OO    I'.M. 

i        1   18  o 

73   '   4  S       cjh.  47111.    10  745 

123 

6657 

"     25 

2.00       " 

i           iS.o 

73      5-2    loh.  47111.    n  835 

107 

6659 

"     25 

3.00       " 

i           18.0 

73      5-7    nh.  39m-    '2935 

93 

6660 

"    25 

4.30       " 

i        1   19.0 

77      6.0    I3h.  09111.'  14455 

181 

6661 

"     25 

7-3"     " 

i           18.0 

73      7.2    i6h.  09111.    17  815 

151 

6663 

"     25 

9.00     " 

I            18.0 

73      7.8    i7h.  39m.    19365 

192 

6664 

"     25     i       ii.  oo 

I 

IS.o 

73      9.0    icjh.  39m.l  21  455 

179 

6665 

26               12.30  A.M. 

I 

18.0 

73      9.5    2ih.  ogm.'  23055 

127  Agitated  surface  of  sand  layer  at 

6666 

"    26          12.45    '                  I 

18.0 

73      6.2    2ih.  2om.   23  245 

385       12.36  A.M. 

6667 

"26           12.50     "                   I 

iS.o 

73    ,   6.3    2ih.  25m.    23  355 

177 

666S 

26              i.oo     "                    i 

iS.o 

73      6.5    2ih.  35m. 

23535 

194 

6670 

"     26             3.00     "                   I 

iS.o 

73      7-8    23h.  35m. 

25585 

137 

6671 

"26               5.00      "                       [ 

18.0 

73      S.S    25h.  35mJ  27695 

142 

6672 

26              6.  ex,     "                     i 

18.0 

73   ,  9.0    26h.  35111.   28  725 

K)6  Closed  outlet  at  6.00  A.M. 

6673 

"26                   7.38       "                            12 

23-5 

95 

oh.  44111.      i  053 

212! 

6675 

"26               11.22       "                          13 

23-5 

95 

oh.  o6m.         138 

295! 

6676 

'•     26           11.27     "                   13 

23.5 

95 

oh.  inn.        2SS 

258 

6677 

"    26         11.37    "               13 

23.5 

95 

•  •  •  .      oh.  21  m.        498 

281 

6678 

"        26        ;           12.00  M.                                 13 

23-5 

95 

.  .  .  .       oh.  44111.      i  ooS 

275  Closed  outlet  at   12.13  P.M. 

6680 

'       26       ,             3.19    P.M.                         14 

18.0 

73 

oh.  07m.         150 

395 

6681 

"      26               3.25      "                      14 

18.0 

73 

oh.  13111.        250 

410 

6682 

"      26               3.38      ' 

14 

18.0 

73 

oh.  26171.         500 

335  Closed  outlet  at  3.40  P.M. 

66,S  ; 

26               5.40 

15 

23-5 

95 

oh.  o6m.         150 

315 

6684 

"      26               5.50      " 

15 

23  5 

95 

oh.  ifim.        370        295 

6685 

"      26               7.30      " 

15 

23-5 

95 

2-5 

ih.  56m.      2690        340;Closed  outlet  at  7.33  P.M. 

6699 

"      27 

5.30A.M.                  19 

23-5 

95 

2.0 

oh.  osm.         1  16     i  020 

6700 

'     27               5.40     "                     19 

23-5 

95 

oh.  ism.        326        690 

6701 

27              6.00     "                     19 

23-5 

95 

oh.  35m.         796        385  Closed  outlet  at  6.00  A.M. 

6703 

"     27 

9.00     " 

20 

23-5 

95 

3-0 

ih.  oom. 

1383        136  Closed  outlet  at  9.05  A.M. 

6704 

"     27             11.33     " 

21 

18.0 

73 

oh.  osm. 

148        260 

0705 

"     27             11.39     " 

21 

18.0 

73 

oh.  14111. 

248        335 

6706 

"     27 

12.00  M. 

21 

18.5 

75 

i  .  7 

oh.  3501. 

5781       320 

6707 

"     27 

I2.3O   I'.M. 

21 

17.0 

69 

i.  9 

ih.  osm. 

i  278        146 

6708 
6709 

27               i.oo 

"    27           1.30    " 

21 
21 

18.0 
19.0 

73 
77 

2.  I 

ih.  35m. 
2h.  osm. 

i  718;       189 
2366        181 

Closed  outlet  at  1.30  P.M. 

6710 

"    27 

2.13       " 

22 

18.0 

73 

oh.  o8m. 

152 

223 

6711 

"     27 

2.18       " 

22 

18.0 

73 

oh.  I3m. 

252 

272 

6712 

"     27             2.32     " 

22 

18.0 

73 

oh.  27m. 

502        198 

6713 

"    27          3.00    '• 

22 

17-5 

71 

oh.  ssm. 

I  012          187 

6715 

"     27 

4.^0       " 

22 

18.5 

75 

2.4 

ih.  som. 

2062          I  ig 

6716 

"    27           5.30    " 

22 

19.0 

77 

3-3 

3h.  2om. 

3722  

6717 

27               S.oo     " 

22 

18.0 

73 

44 

5h.  5om. 

f>442,  

6718 

"     27              9.00 

22 

18.0 

73 

6h.  5001. 

7494        218 

Closed  outlet  at  9.00  P.M. 

"794 

July     i               5.  m     " 

32 

23-5 

95 

2.0 

oh.  o6m. 

158          84 

6795 

"        i 

5.30       " 

32 

23-5 

95 

2.2 

oh.  36m. 

938          92 

366 


WATER   PURIFICATION  AT  LOUISVILLE. 


RESULTS    OF    BACTERIAL   ANALYSES—WITH    ELECTROLYTICALLY    PREPARED    HYDRATE  OF 

IRON.  —  Concluded. 


Collected. 

Rate  of 

j 

u 

Filtr 

ition. 

£ 

C 

•~ 

1 

Number       o- 

|s. 

^ 

Period  of        •*•  jy. 
Service  Since     tJ  c 

3 

(J  j 

B 

of            - 

5 

\V       1  '                  >   -  ^ 

V  w 

Remarks. 

Run. 

V   V 

(i"  b  1 

I 

Ho'urs'and      *^'1' 

?s 

J 

Dale. 

Hour. 

3 

§^i 

'o 

Minutes.        "s'J 

'E'i 

•§ 

;  -is 

i=  a« 

1 

^25     %u 

* 

u 

s 

J 

I   &.                  03 

1897 

6796 

July 

S.OO    P.M. 

132      23.5 

95 

2-9 

3h.  o6m.       4  308        39 

6798 

9.00       '^ 

132      23.5 

95 

3-4 

4h.  o6m. 

5  678        49 

67(1(1           " 

5h.  o6m. 

u  /  yy 

6800 

1  I  .  OO       " 

132          23  •  ;> 

132   ,  23.5 

95 

4*  3 
4-7 

oh.  o6m. 

8  448         94 

6801 

I2.OO  M. 

132   i  23.5 

95 

5-0 

7h.  06111.       9  858        87 

6927 

4-39  A.M. 

147   i  23.5 

95 

oh.  0501.           140      420 

6928 

4-44      ' 

147     23.5 

95 

oh.  lorn.           240 

360 

6929       " 

4.55    ' 

147 

23.5 

95 

oh.  21  m.          490 

325 

6932                9 

5.20       " 

T47 

23.5 

95 

oh.  46m.        i  090 

244 

f'933                9 

6.30     " 

147            20.0 

Si 

2.  2 

ih.  56m.        2  510 

154 

6934                9 

S.oo     " 

147        iS.o 

73 

24 

3(1.  26m.        4  1  60 

259    Closed  outlet  at  8.14  A.M. 

6935                9 

8.55      " 

148    '  18.5 

75 

oh.  oSm.    i       152 

226 

6936        "       9 

9.02     ' 

148        18.0 

73 

oh.  ism.          302 

212 

f'937                9 

148     '   18.0 

73 

'•7 

oh.  43m.    i       908 

I76 

6940                9 

IO.OO       " 

148        iS.o 

73 

i-9 

ih  .  13m. 

1338 

124 

6941                  9 

I  I  .  OO       " 

148        iS.o 

73 

2.  I 

2h.  13111.        2  41^ 

88 

''942                  9 

12.  OO  M. 

148 

iS.c 

73 

3-0 

3h.  13111.       3488 

S3 

6943                  9 

1.  00   P.M. 

148        iS.o 

73 

3-5 

4h.  13111. 

4  558 

96 

6952                  9 

".39      " 

150           20.0 

Si 

oh  .  08  in  .           153 

315 

f>953                  9 

11.41    ' 

150        20.  o 

Si 

oh.  13111.           253 

340 

6954                  9 

12.00       " 

150           2(3.0 

Si 

oh.  2gm. 

443 

555  jClosed  outlet  at  12.00  P.M. 

6956          '      10 

I.I9  A.M. 

151        iS.o 

73 

oh.  08111.           147 

330 

6957          '      10 

1.24       " 

151        iS.o 

73 

oh.  13111.           247 

430 

6959:        '      10 

I.3S       " 

151         iS.o 

73     

oh.  2/m. 

497 

340 

6960        "     i  o 

2.OO 

151         18.0 

73 

oh.  49111. 

907 

173    Closed  outlet  at  2.00  A.M. 

6961 

'        10 

2.40       " 

152        18.0 

73 

oh.  I5m.           251 

275 

6962 

"      10 

2.45     ' 

152     ,   iS.o 

73 

oh.  2om.          351 

275 

6963 

"        10 

3.oo     " 

152        18.0 

73  !•••• 

oh.  35111.          601 

269    Closed  outlet  at  3.10  A.M. 

7234            '       22 

1.20   P.M. 

177        23.0 

93    .... 

oh.  oom.    ;        154 

151 

7235           "       22 

1.30       " 

177     i   23.0 

93 

2.  I 

oh.  1  6m. 

394 

174 

7236 

'       22 

2.00       " 

177 

23.0 

93 

2.  I 

oh.  46m. 

1084 

202 

Closed  outlet  at  2.00  P.M. 

7238 

"       22 

3.09       " 

178 

23.0 

93 

oh.  o6m. 

149 

139 

7239 

"        22 

3.24       ' 

178        23.0 

93 

oh.  2im. 

499 

138 

7-1' 

"       22 

5.00       " 

178 

23-5 

95 

2-3 

ih.  57m. 

3449 

63 

7242 

"       22 

S.oo     " 

178 

23.5 

95 

3-7 

4h.  57m. 

6899 

38 

7257 

"       23 

9.58  A.M. 

181 

23.5 

95 

oh.  o6m. 

146 

165 

7258 

23 

IO.I3       " 

181 

23   5 

95 

oh.  2im. 

496 

139 

7259 

'       23 

11.00       " 

181 

23-5 

95 

2.2 

ih.  oSm. 

i  596 

128 

7260 

"       23 

I2.IX3  M. 

181 

23.5 

95 

2-7 

2h.  oSm. 

3  >'O6 

in 

7261 

'       23 

I.OO    P.M. 

181 

23-5 

95 

3-0 

3h.  o8m. 

4386 

116 

7262 

'       23 

2.00       " 

181 

23.5 

95 

3-6 

4h.  oSm. 

5806 

90 

7263 

"       23 

3.00       " 

181 

23.0 

93 

4.0 

5h.  o8m. 

7  206 

163 

Closed  outlet  at  3.10  P.M. 

INVESTIGATIONS  OF  THE   WATER  COMPANY  FROM  APRIL   TO  JULY,  1807.  367 


Summary  of  Results,  showing  the  Amount  of 
Suspended  Matter  and  Number'  of  Bacteria 
in  the  River  Water  as  it  passed  througli 
the  several  Settling  Basins. 

In  this  table  are  given  all  of  the  determina 
tions  of  the  amount  of  suspended  matter  and 
number  of  bacteria  in  the  effluents  from  the 
several  settling  basins,  together  with  corre 
sponding  determinations  of  the  river  water. 
It  will  be  seen  that  in  several  instances  the 
determinations  in  the  case  of  the  effluents 
gave  larger  results  than  were  found  with  the 
river  or  with  the  effluent  from  preceding  ba 
sins.  This  is  mainly  accounted  for  by  the 
fact  that  it  was  not  found  practicable  to  col 
lect  samples  from  the  same  water  as  it  passed 
through  the  system,  but  all  samples  from  the 
settling  basins  were  taken  at  the  same  time, 
and  are  tabulated  with  samples  of  river  water 
collected  from  one  to  three  hours  earlier. 
The  samples  do  not,  therefore,  represent  the 
actual  condition  of  the  same  water  as  it 
passed  through  the  system,  but  the  condition 
of  the  various  effluents  at  the  hour  given. 

All  of  the  columns  given  are  explained  by 
their  headings,  except  that  headed  "  Treat 
ment."  Under  this  heading  and  subheading 
"  Kind,"  two  letters  are  given.  The  first  let 
ter  refers  to  the  kind  of  coagulant  used,  and 
the  second  to  the  place  of  application.  These 
letters  refer  to  coagulants  and  places  as  fol 
lows: 

Kind  of  Coagulant. 

A.  Hydrate  of  alumina  from  sulphate  of 
alumina. 


B.  Hydrate   of   iron   from   persulphate   of 
iron. 

C.  Hydrate   of  alumina  prepared  electro- 
lytically  from  aluminum. 

I).   Hydrate   of   iron   prepared   electrolyti- 
cally  from  iron. 

E.  Hydrate  of  iron  from  protosulphate  of 
iron. 

F.  E.  with  caustic  soda.      The  soda  was 
applied  at  basin  No.  2,  and  the  copperas  at 
the  Jewell  settling  chamber. 


Place  of  Application. 

A.  Basin  No.  2  and  Jewell  settling  cham 
ber,  in  equal  amounts. 

B.  Jewell  settling  chamber. 

C.  Top  of  filter. 

D.  Basin  No.  I  and  Jewell  settling  cham 
ber. 

E.  Basin  No.  I  and  top  of  filter. 

F.  Basin  No.  i. 

G.  Basin  No.  2. 

Coagulants  were  always  applied  at  the  inlet 
pipes. 

Under  subheading  "  Amount "  the  total 
amounts  of  chemicals  used  are  given  in 
grains  per  gallon  in  the  case  of  commercial 
chemicals  and  in  ampere  hours  per  gallon  in 
the  case  of  electrolytic  treatment;  and,  in  the 
case  of  application  at  1)  or  E,  the  separate 
amounts  are  given  as  foot-notes  in  the  order 
in  which  they  were  applied,  the  upper  one 
being  first  and  the  lower  second. 

Where  a  settling  basin  was  not  in  use  the 
fact  is  so  recorded  in  the  column  for  that 
basin. 


368 


WATER    PURIFICATION   AT  LOUISVILLE. 


AMOUNT    OF     SUSPENDED     MATTER    AND     NUMBER    OF    BACTERIA    IN    THE    RIVER   WATER   AS 
IT    PASSED    THROUGH    THE    SEVERAL    SETTLING-BASINS. 


Date 

1897. 

Trea 

men, 

RiVL 

r  Water. 

F.frl 
Basi 

nent  of 
i  No.  i. 

Efflu 
Basin 

ent  of 
No.  2. 

Effluent 
Settling 

of  Jewell 
Chamber. 

Day. 

Hour. 

c 

3 

B! 

6 
P 
'/. 

•2 

p 

1 
<. 

1  1 
is. 

at; 
3p! 

'3 

U  u- 

g 

-  C_j 

•  c 
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T3  — 

°-b 

3  £. 

5 

U  u 

^O 
03 

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x  "A 

~v  i- 

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D 

u  c 

u  _ 

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pa 

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c^t 
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n 

A  ril 

I)  A 

084 

784 

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14 
15 
16 

"    20 
21 

"    22 
24 
"    26 
27 
"    28 

10.30   " 
10.00  " 

1.  00   " 

9.30  •' 

4.00  " 

3.30  " 

2.30  " 
9.30  " 

9.00  " 

25 
28 
31 
32 
34 
35 
43 
45 
46 
48 

B-A 

A-A 
B-A 
D-A 
D-A 
B-A 
A-A 
C-A 
D-A 
C  A 

2.83 
3  oi 
3-37 
.080 
.136 
i.  Si 
1.44 
.030 
.078 

322 
347 
407 
205 
183 
231 
196 
184 
1  60 

38  TOO 
28  700 
37  ooo 
1  6  800 

12  6OO 

14  600 

9400 

7  4<)<) 
II  700 

185 
216 
268 
151 
192 
295 
133 
107 
"5 

47900 

34  500 
29  500 
1  8  700 
10  700 

12  IOO 

4  ooo 
3900 
II  400 

225 
237 
1  66 
1  60 

120 
131 
1  06 
71 
I  19 
82 

24  200 

31  700 

14  ioo 

19400 
7900 

5  600 
4  200 
2  400 

I  2  900 

87 
129 
73 
128 
97 
95 
80 
50 
Si 

ii  200 
ii  500 
3  50<) 
ii  800 
7300 
3  900 
2  900 
i  Soo 

IO  2OO 

"    28 
29 

3<> 
3" 
May   I 

!'    7 

4.00  P.M. 
II.  OO  A.M. 
3.00  I'.M. 

9.  oo  " 

3-OO   " 
5.OO  A.M. 
10.30   " 

49 
50 

52 
53 
54 
56 

57 
58 

C-A 
A-A 
C-A 
C-B 
C-G 
C-A 
C-A 
C-A 

.014 
1.17 
.019 
.019 
.019 
.048 
.040 
.028 

133 
136 

77 
77 
77 
453 
453 
4^3 

19  500 
14  800 

IO  2OO 

9700 
7900 
51  500 

31  ioo 

107 
127 
76 
68 
59 
181 
175 
1/5 

22  4OO 

1  5  Soo 

R  IOO 

8  Soo 
7  Soo 
35  900 
19  600 

92 

116 

47 
67 
74 

38 

212 

23  ioo 

S  200 

6  300 
9  ioo 
6  ioo 
36  200 

2  OOO 
2  IOO 

76 
S3 
34 
37 
47 

104 
115 

14  900 

5  800 
3  Soo 
4300 
4  600 
33  ioo 
7  100 
8  Soo 

7 
8 
"    8 
8 
9 
19 
20 
"    22 
"    22 

IO.OO   " 
4.00  A.M. 
9.30   " 
4.30  P.M. 
4.30  A.M. 
11.00  I'.M. 
5.30   " 
3.OO  A.M. 
9.OO  I'.M. 

59 
60 
6  1 
63 

66 
67 
68 
70 
70 

A-A 
A-A 
A-A 
A-A 
A-G 
G-A 
G-A 
G-A 
G-A 
G  A 

2.47 
3.02 
3.6o 
3-6? 
3-75 
1.96 
1.92 

1.  12 
1.  12 

30 
3° 
3° 
30 

3" 

273 
277 
263 
255 

28  500 
19  loo 

24  2OO 

21  IOO 

13  ioo 

13  400 

10  500 
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7400 

172 

168 
157 
148 
no 

201 
195 
M4 

138 

27  900 
25  500 
23  200 
20  200 

14  200 

1  3  600 
9  200 

I  I  OOO 
IO  OOO 

153 
147 

88 
83 
"5 
184 
170 
139 
128 

5  ioo 
0650 

O  IOO 

9400 

10  800 
8  900 
8  Soo 
9900 
5  Soo 

94 

84 
SS 
72 
84 

122 

99 

122 
90 

12  OOO 

8  500 
6  ioo 
6  200 
9300 
6  200 

5400 

6  400 

3900 

25 
26 

28 

5.00  A.M. 
8.30  P.M. 
3.00  A.M. 

75 
81 
87 

G--A 
G-A 
G-A 
G  C 

o.So 
o  92 

1.26 

"3 

IOO 

98 

9300 
18  200 
6  700 

1  08 

86 
92 

8  800 
15  700 
6  900 

79 

77 

102 

6  300 
IO  IOO 

6  too 

55 
75 
85 

5  500 
8  400 

5  200 

G  B 

G  G 

lS4 

166 

:'.:::::: 

,, 

08 

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I  46 

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Not 

• 

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165 

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581 

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64 

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158 

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12.00  M. 

13 

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D  A 

0.038 

425 

413 

426 

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237 

28l 

"   26 

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16 

A  A 

"   27 

I2.3O  A.M. 

17 
18 

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A  A 

2.00 

622 
673 

583 

620 

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of 

586 

567 

D  A 

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65 

"   28 

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A  A 

94 

26 

A  A 

408 

389 

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g.OO  P.M. 
6.IO  A.M. 
11.30   " 

30 
31 
31 

A-A 
A-A 

A  A 

2.98 
2.52 
2.52 

308 
297 
279 

6  ioo 
4  900 
4900 

297 
280 
256 

4  700 
4  600 

250 
253 

248 

4  200 

144 

112 

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2  600 

I  300 

UNIVE 


INVESTIGATIONS  OF  THE   WATER  COMPANY  FROM  APRIL   TO  JULY,  /-V//7.   369 

SUSPENDED    MATTER    AND    BACTERIA.  —  Concluded. 


1).  ill- 

Trea 

Riv 

r  Water. 

Effl 

uent  of 

Eft 

uent  of 

Kffluei 

t  of  Jewell 

Has 

n  No.  i 

Bas 

n  .So.  -2. 

Setilin 

-Chamber. 

= 

S 

II 

3 

U  ^ 

1  0 

o  — 

1 

II 

u  u. 

II 

1 

Day. 

Hour. 

U 

^ 

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s 

Is. 

f! 

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j^ 

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3  £ 

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lulv  I 

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1  32 

D-.A 

0.078 

2lS 

2  900 

214 

IT  r 

2  2OO 

116 

J  u  1  V    1 

2 

6.OO  A.M. 

T33 

C-A 

0.037 

I  59 

2  2OO 

172 

1  900 

167 

71 

I  OOO 

I  2  .  (X)  M  . 

i  ^ 

C-A 

0.028 

151 

2  2IO 

148 

2  1  OO 

no 

"    2 

8.30  P.M. 

i36 

A-B 

5  000 

140 

6  ioo 

128 

4  600 

62 

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5.30  A.M. 

137 

A-C 

2.06 

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4  Soo 

143 

4300 

139 

2  500 

170 

I  400 

6 

4.30  P.M. 

140 

A-B 

1.67 

121 

3  900 

7  1 

I  3IO 

6 

9.00   " 

140 

A-B 

1.67 

127 

3  800 

57 

I  7OO 

"   7 

1  1  .  OO  A.M. 

141 

A-C 

i.  59 

552 

12  IOO 

191 

3  700 

*  '   7 

2.30  P.M. 

142 

A-C 

2.  02 

753 

12  6oO 

324 

6  600 

"   7 

4  .  oo  '  ' 

142 

A-C 

2-O2 

343 

13  ioo 

226 

3  7oo 

"   7 

10.00  " 

144 

A-C 

2.6o 

455 

400 

3  45° 

8 

4.OO  A.  M. 

145 

A-B 

1  .92 

438 

14  ioo 

i  355 

8 

3-OO  P.M. 

146 

A-B 

1  .99 

633 

1  7  900 

M3 

3  300 

"   9 

5  OO  A.M. 

147 

D-B 

.089 

488 

7300 

Not 

in  use 

Bas 

in  No.  2 

181 

3400 

'   9 

10.00    " 

MS 

D-B 

•099 

419 

5  900 

was 

not  used 

138 

2  IOO 

'   9 

5.OO  P.M. 

149 

A-B 

2.41 

455 

6  300 

"  " 

again 

after  Run 

lift 

i  400 

'   9 

9.00  " 

149 

A-B 

2.4! 

478 

7400 

No.  i 

,6. 

148 

i  890 

'   9 

12.00   " 

150 

D-B 

.09! 

445 

S  500 

"  " 

'57 

2  300 

"   IO 

1.30  A.M. 

151 

D-B 

.  .096 

430 

9  ooo 

84 

2  150 

"   10 

3.00   " 

152 

D-B 

.104 

312 

9  600 

123 

I  700 

'  '   IO 

5.OO   " 

1  53 

A-B 

2.69 

32O 

"   IO 

9.00   " 

153 

A-B 

2.6g 

384 

7  100 

124 

850 

"   IO 

2.30  P.M. 

155 

B-B 

2.66 

379 

9400 

"  " 

85 

2  900 

"   10 

5.40   " 

156 

A-B 

2.69 

305 

9400 

142 

3  ioo 

"  14 

9.30   " 

157 

A-D 

1.85' 

9' 

5  600 

186 

3  900 

92 

i  380 

"  14 

11.30  " 

i5s 

A-E 

1-81' 

95 

5  600 

182 

4  600 

77 

4400 

"  15 

5  00  A.M. 

159 

A-D 

2.22:' 

99 

5900 

183 

4  700 

107 

2  2OO 

"  15 

9  oo  " 

159 

A-D 

2.22:1 

71 

4600 

IOO 

2  7OO 

71 

Soo 

"  15 

10.30  " 

1  60 

A-B 

2.IS4 

71 

4600 

127 

4  600 

(>s 

I  IOO 

"  15 

3.00  P.M. 

161 

A-E 

2.ig5 

So 

6  ioo 

'54 

3  900 

124 

2  4OO 

"  15 

8.00  " 

162 

A-D 

2.  16* 

85 

6  ioo 

135 

i  930 

7' 

J  210 

"  15 

11.30  " 

163 

A-E 

2.19s 

89 

6000 

142 

2  5OO 

139 

I  700 

1  16 

4.00A.M. 

164 

A-B 

I.  Si 

89 

5  800 

Not 

in  use 

1  20 

980 

"  16 

II.OO   " 

1  66 

A-B 

2.14 

89 

5  300 

" 

9i 

i  500 

"  16 

10.05  P.M. 

167 

A-B 

2.82 

29 

59oo 

" 

"  " 

79 

760 

"  17 

4.30A.M. 

168 

A-D 

2.32' 

52 

6400 

23 

940 

o 

840 

"  17 

2.OO  P.M. 

1  68 

A-D 

2.32' 

31 

6  ioo 

71 

i  400 

3° 

I  190 

"  =7 

5.30   " 

169 

A-E 

2.30" 

25 

6  ioo 

55 

i  250 

25 

I  180 

"  17 

12.  OO   " 

169 

A-E 

2.30' 

19 

5  600 

39 

i  150 

17 

680 

"  18 

6.OO  A.M. 

170 

A-D 

2  2O9 

13 

4  5°o 

26 

20 

810 

"  18 

II.OO   " 

170 

A-D 

2.299 

09 

3900 

26 

gSo 

22 

770 

"  18 

5.30  P.M. 

171 

A-E 

2.32'0 

oS 

4800 

42 

780 

33 

770 

"  18 

I2.OO   " 

172 

A-D 

2.  IS" 

09 

3900 

'9 

Sio 

6 

730 

"  '9 

10.00  A.M. 

172 

A-D 

2.18" 

20 

3  800 

37 

i  080 

17 

810 

"  '9 

9.30  P.M. 

173 

A-F 

I.5I 

78 

34oo 

16 

590 

20 

57" 

"  '9 

12.00  M. 

173 

A-T 

I.5I 

78 

3000 

M 

860 

18 

700 

"   20 

5.00  A.M. 

173 

A-F 

1.51 

75 

2  7OO 

21 

SSo 

If) 

495 

"   20 

4.00  P.M. 

'73 

A-F 

'•51 

66 

3250 

SI 

l  020 

31 

960 

"   20 

10.00  " 

1/4 

A-B 

1.  60 

70 

2  550 

Not 

in  use 

49 

I  1  20 

"   21 

9-00  A.M. 

174 

A-B 

1.  60 

76 

3350 

43 

2  I  So 

"   21 

3.30  P.M. 

'75 

A-C 

1.  60 

130 

4  850 

••  " 

86 

2  780 

"   21 

II.OO  " 

176 

A-B 

1.02 

130 

4  250 

70 

I  670 

"   22 

5-00   " 

178 

D-B 

.040 

128 

4780 

15 

3400 

"   22 

II.3O   " 

'79 

A-C 

1.04 

127 

4  800 

37 

I  900 

"   23 

1  .  3O  A  .  M  . 

1  80 

A-D 

0.7S 

140 

4600 

" 

"  " 

1  300 

"   23 

9.00  P.M. 

182 

A-G 

9-77 

'7' 

6  200 

84 

3400 

82 

3  600 

;'  23 

II.OO  " 

183 

A-B 

0.77 

173 

6  200 

Not 

in  use 

35 

3800 

3.30  A.M. 

184 

A  C 

I.  10 

174 

5  300 

163 

24 

"  24 

5.30  " 

185 

A-B 

1.03 

'  1  *t 
173 

5300 

•• 

..  .. 

108 

37° 


WATER   PURIFICATION  AT  LOUISVILLE. 


Final  Summary,  showing  the  Leading  Results 
of  Operation. 

In  the  following  table  will  be  found  a  sum 
mary  of  all  of  the  leading  results  of  opera 
tion  of  the  Water  Company's  devices.  The 
devices,  methods  of  operation,  and  general 
periods  of  operation,  have  already  been  pre 
sented,  as  well  as  complete  tables  of  analy 
tical  results,  it  is  only  necessary,  therefore, 
to  explain  the  various  headings  in  the  table. 

Settling  Basins  in  Service.  —  Under  this 
heading  the  basins  used  for  preliminary 
treatment  of  the  water  previous  to  its  en 
trance  to  the  Jewell  settling  chamber  are 
given.  It  is  understood  that  the  latter  was 
in  use  at  all  times. 

Treatment. — For  economy  of  space  letters 
have  been  used  in  the  two  columns  un 
der  this  head.  The  letters  refer  to  the  co 
agulant  used,  or  place  of  application,  as 
follows: 


A.  Hydrate  of  alumina  from  sulphate  of 
alumina. 

B.  Hydrate    of   iron    from    persulphate    of 
iron. 

C.  Hydrate   of  alumina   prepared   electro- 
lytically  from  aluminum. 

D.  Hydrate   of   iron    prepared    electrolyti- 
cally  from  iron. 

E.  Hydrate  of  iron  from  copperas. 

F.  K.  with  caustic  soda.     The  caustic  soda 
was  applied  to  basin  No.  2,  and  the  copperas 
at  the  inlet  to  the  Jewell  settling  chamber. 


A.   Equal  amounts  at  basin  No.  2  and  Jew 
ell  settling  chamber. 

1).  Jewell  settling  chamber. 

C.  Top   of   filter.      (Outlet    of   Jewell    set 
tling  chamber. 

D.  Basin  No.   T  and  Jewell  settling  cham 
ber. 


E.   Basin  No.   i  and  top  of  niter. 
E.   Basin  No.  i. 

G.   Basin  No.  2. 

In  all  cases  coagulant  was  applied  at  the 
inlets  of  the  settling  basins  or  chamber,  un 
less  otherwise  recorded. 

Grains  of  Chemical  per  (iallon.  —The  total 
amount  of  chemical  used  per  gallon  of  ap 
plied  water  is  given  under  this  heading. 
\Vhere  it  was  applied  at  more  than  one  point 
the  separate  amounts  are  given  as  foot-notes 
in  the  order  they  were  applied. 

lilectric  Current. — The  electric  horse-power 
per  million  gallons  of  treated  water  per  24 
hours  is  given  from  calculations  based  on  the 
amperage  and  voltage  of  the  electric  current. 
Ampere  hours  of  electric  current  per  gallon 
of  treated  water  is  used  to  express  the 
amount  of  electrolytic  treatment.  For  the 
amounts  of  metal  used  see  discussion  in  the 
last  portion  of  this  chapter  on  the  rate  of 
electrolytic  decomposition  of  the  metal. 

Average  Suspended  Solids. — In  so  far  as 
was  feasible,  the  suspended  solids  in  the  river 
water,  and  in  the  water  above  the  sand  layer 
in  the  filter,  were  determined  for  each  run. 
The  results  are  given  in  these  two  columns. 

The  headings  in  the  balance  of  the  table 
have  already  been  described  in  Chapter  VIII, 
and  do  not  need  further  explanation. 

On  runs  Nos.  154  and  155  the  free  acid  in 
the  persulphate  of  iron  was  neutralized  by 
caustic  soda. 

Several  runs  were  not  continued  to  their 
normal  length,  owing  to  either  the  comple 
tion  of  the  special  study  for  which  the  run 
was  made,  the  necessity  of  taking  up  other 
work  at  a  certain  time,  or.  in  two  cases,  by 
closing  operations  for  the  week.  Where  the 
run  ended  on  a  good  water  for  these  reasons, 
the  period  of  service  is  marked  with  a  star  (*); 
and  it  is  to  be  noted  that  in  most  of  these 
cases  the  bacterial  efficiency  is  probably  lower 
than  it  would  have  been  had  the  run  been 
continued  to  its  normal  end,  as  the  samples 
collected  at  the  beginning  of  the  run  gener 
ally  represented  the  poorest  water  of  the  run. 


INVESTIGATIONS  OF  THE   WATER  COMPANY  FROM  APRIL   TO  JULY,  1.S97.  371 


§12 

?:'££ 


O       O'OOOO'OGC 


t    ;  O  N  O 


o  o  q 
coo 


88883 83888888 88 8 


jodoj,iv 


£  E  E  £  £  E  E  E  E  E  E  £  E  J  E  E  E  E  £  E  £  E  E  E  |  E  £  E  E  |  E  E  £  E  £  E  E  £  E  £  |  £  E 


O   O   M     •     -000000" 


.     S.     SS.     S  .    .     S.     S  S  S  S  .     X  .    . 

'   £~   *.  i-'   <~  ~   -~  '   <. -~  <  i.'   •<.'" 


WATER   PURIFICATION  AT  LOUISVILLE. 


INVESTIGATIONS  Ol-    THE   WATER  COM  PA  NY  FRO  At  APRIL   TO  JULY,  18W.  373 


.30  i 
i'.H  = 


III 


O  O  O      O 


O  «  Of 


S  8 


2  a 


^  jnm'i-iL'uuv 


o"  o  o1  o" 


•  -r        f  ~-  c>  r^  m  -f-  o 

•  O     •    O    O   O    O    O   O     • 


374 


WATER   PURIFICATION  AT  LOUISVILLE. 


z  :  :  :  °  :  :  z  :  :  ss 

'.:•••  i  :  .  js 


O      vO  O      •      •      O      CO    HI  O 


>  O      •     •       O 


O     •      •       O      O 


v.     •      -Oi-O 


:  s  R  :   :•« 


O  O>     •    i-i  O    t 
1§   O      •    O    O    i- 


INVESTIGATIONS  OF  THE   WATER  COMPANY  FROM  APRIL   TO  JULY,  1807.  375 


at  •  a 


C 

i   !     Ul 

2i&3 

s  r 

s  ! 

D 
en 


»  O    »/i  O   l^  u-i  O    c*l  O 


"-   r  -7  .' 
<  3"  " 


,-?.     I   •J3)ITA\    J3A1JJ 


ft:         O  •  O 

O   O     •     •   O 


O&-  —  U  —  XX'OXXXXU  — 


a- o  —  w  m -r  i 


OUTLINE   OF   THE    METHOD    FOLLOWED    IN 

THE  DISCUSSION  OF  THE  RESULTS  OF 

THESE  INVESTIGATIONS. 

In  the  following  pages  are  presented  the 
full  discussions  of  the  results  of  the  investi 
gations  made  during  1897  U1  connection  with 
the  devices  arranged  by  the  Water  Company, 
or  in  connection  with  laboratory  experiments 
on  a  small  scale.  These  discussions  are  pre 
sented  in  fifteen  main  sections  as  follows: 
Section  No.  i.  Purification  of  the  Ohio 

River  water  by  plain  sedimentation. 
Section  No.  2.  Account  of  the  commercial 
chemicals  available  as  coagulants  for  the 
( )hio  River  water,  and  of  the  manner  of 
their  behavior  when  applied  to  this 
water. 

Section  No.  3.  Status  at  the  beginning  of 
this  portion  of  the  investigation,  with  a 
general  description,  of  the  formation  of 
coagulating  chemicals  by  the  electro 
lytic  decomposition  of  metal  plates. 
Section  No.  4.  Detailed  account  of  the  elec 
trolytic  formation  of  iron  hydrate  in  the 
Ohio  River  water. 

Section  No.  5.  Detailed  account  of  the  elec 
trolytic  formation  of  aluminum  hydrate 
in  the  Ohio  River  water. 

Section  No.  6.  Relative  efficiency  of  available 
coagulants  based  on  equal  weights  of 
metal  used,  and  also  on  the  amount  of 
electric  current  in  the  case  of  electro- 
lytically  formed  coagulants. 
Section  No.  7.  Economical  application  of 
coagulants,  in  terms  of  sulphate  of  alu 
mina,  to  aid  in  the  removal  of  suspended 
matter  by  sedimentation. 
Section  No.  8.  Effect  of  the  period  of  co 
agulation  of  the  Ohio  River  water  be 
fore  filtration. 

Section  No.  9.  Degree  of  coagulation  of  the 
water  before  filtration  and  the  minimum 
amount  of  coagulant  required  for  that 
purpose. 

Section  No.  10.  On  the  conditions  of  suc 
cessful  filtration. 

Section  No.  u.  Quality  of  the  effluent,  after 
proper  sedimentation,  coagulation,  and 
filtration — independent  of  the  nature  of 
the  coagulant. 


376 


WATER  PURIFICATION  AT  LOUISVILLE. 


Section  Xo.  12.  Manner  in  which  the  nature 
of  the  coagulant  affected  the  quality  of 
the  effluent. 

Section  No.  13.  Amounts  of  the  different 
available  coagulants  which  would  be  re 
quired  with  optimum  conditions  of  sub 
sidence  and  filtration  to  purify  satisfac 
torily  the  Ohio  River  water. 

Section  No.  14.  Degree  to  which  the  several 
coagulants  in  their  respective  amounts 
would  affect  the  quality  of  the  effluent, 
with  its  practical  significance,  and  a  con 
sideration  of  the  advisability  and  cost  of 
the  removal  of  the  added  constituents. 

Section  No.  15.  Relative  costs  of  equivalent 
amounts  of  the  different  available  co 
agulants,  together  with  an  estimate  of 
the  yearly  cost  for  coagulants  for  the  pu 
rification  of  the  Ohio  River  water. 

SECTION   No.    i. 

PURIFICATION  OF  THE  OHIO  RIVER  WATER 
BY  PLAIN  SEDIMENTATION. 

Plain  sedimentation  means  the  removal  of 
suspended  matters  from  the  water  by  gravity 
in  the  absence  of  any  coagulating  treatment. 
In  many  cases  in  this  report  subsidence  is 
used  synonymously  with  sedimentation;  and 
in  some  places  other  expressions,  such  as  set 
tling  and  settlement,  are  also  used  in  refer 
ring  to  this  same  action. 

In  the  early  summer  of  1896  a  series  of 
sedimentation  experiments  upon  a  ^  small 
scale  were  undertaken  to  show  the  relation  of 
coagulation  and  period  of  subsidence.  The 
results  of  these  experiments  have  been  re 
corded  in  Chapter  IV,  where  it  will  be  seen 
that  a  number  of  them  throw  light  upon  the 
present  question.  As  a  matter  of  conven 
ience,  the  results  of  those  experiments  in 
which  no  coagulants  were  used  are  repeated, 
as  follows: 


Percentage  Removal. 

Parts 

per  Million. 

-24  Hours. 

48  Hours. 

590 

936 

320 

220 

52 

32 
41 

.    73 
64 
62 
60 

26l 

44 

74 

Averages 

469 

41 

67 

From  a  practical  point  of  view  the  condi 
tions  under  which  the  above  experiments 
were  carried  on  were  abnormal  in  two  re 
spects.  In  the  first  place,  the  diameter  of  the 
tank  (2  feet)  was  such  that  the  friction  of  the 
water  upon  the  sides  caused  the  vortex  mo 
tion  of  the  suspended  particles  to  decrease 
more  rapidly  than  in  large  basins  or  reser 
voirs;  or,  in  other  words,  it  caused  the  water 
to  reach  a  state  of  rest  more  quickly.  Owing 
to  the  fact  that  subsidence  is  very  closely  as 
sociated  with  the  vortex  motion  of  the  par 
ticles,  the  above  results,  so  far  as  this  point 
is  concerned,  show  higher  percentages  of  re 
moval  than  would  occur  in  practice.  Sec 
ondly,  the  high  and  varying  temperature  of 
the  boiler-house  in  which  the  tank  was  placed 
caused  the  presence  of  currents  which  re 
tarded  the  subsidence  by  increasing  the  vor 
tex  motion. 

The  significance  -of  these  points  is  shown 
clearly  by  the  results  of  plain  sedimentation 
experiments  made  in  one-gallon  bottles, 
which  were  kept  at  approximately  the  same 
temperature.  It  will  be  noted  that  the 
average  amount  of  suspended  matter  in 
these  experiments  was  substantially  the  same 
as  in  the  case  of  those  recorded  in  the  last 
table;  and  the  general  character  of  the  water 
was  fairlv  similar. 


R           1 

r  w  ,,cr 

Parts  per  Million. 

24  Huurs.             48  Hours. 

521 

81                        84 

5,6 
472 
428 
33S 

So                      86 
76                      80 
71                       86 
77                       86 

A 

verages         455 

77                       S4 

In  addition  to  showing  that  by  24  hours 
of  quiescent  subsidence  about  75  per  cent,  of 
the  suspended  matter  in  fairly  normal  muddy 
water  may  be  removed,  the  above  results 
demonstrate  that  under  these  conditions  eco 
nomical  subsidence  cannot  be  carried  beyond 
this  period  (24  hours).  Comparing  the  last 
results  with  those  in  the  first  table,  it  is  clear 
that  the  conditions  of  subsidence,  as  already 
noted,  were  important  factors,  and  that  24 
hours'  subsidence  in  gallon  bottles  was  more 
efficient  than  48  hours  in  the  settling  tank 


SUMMARY  AND   DISCUSSION   OF  DATA    OF  1S!>7. 


377 


placed  in  the  boiler  house.  In  this  connec 
tion  it  may  be  stated  that  some  analyses  made 
in  June,  1896,  of  the  water  leaving  the  Cres 
cent  Hill  reservoir,  which  holds  about  6  days' 
supply,  indicated  a  removal  by  subsidence  of 
about  60  per  cent,  of  the  suspended  matters 
in  the  general  class  of  water  under  considera 
tion. 

Concerning  the  efficiency  of  basin  No.  i 
in  the  removal  of  suspended  matters  by  plain 
subsidence,  the  summary  of  results  on  pages 
371  to  375  show  that,  during  the  early  spring, 
when  the  suspended  matter  was  rather  coarse, 
the  removal  ranged  from  20  to  50  per  cent., 
when  the  basin  held  about  3  hours'  supply. 
\Yith  the  water  later  in  the  spring,  and  in  the 
summer,  when  the  suspended  particles  were 
much  finer,  the  removal  of  suspended  matters 
in  this  basin  ranged  from  o  to  15  per  cent., 
but  for  the  most  part  the  water  as  it  left  this 
basin  showed  no  substantial  purification. 

With  regard  to  the  removal  of  bacteria  by 
plain  subsidence,  the  influence  of  the  tem 
perature  is  considerable.  In  general  terms  it 
appears  that  the  percentage  removal  of  bac 
teria  follows  quite  closely  that  of  the  sus 
pended  lifeless  particles.  This  is  to  be  ex 
pected,  because  the  bacteria  to  a  considerable 
degree  appear  to  be  attached  to  the  grosser 
suspended  particles.  The  removal  of  bacteria 
by  plain  subsidence  is  not  a  very  important 
factor,  however,  because  with  little  or  no  ex 
tra  expense  to  the  general  process  they  may 
be  removed  subsequently  by  the  necessary 
coagulation  and  nitration. 

The  character  of  the  suspended  matter  in 
the  river  water  is  a  point  of  great  importance 
in  purification  by  subsidence;  and,  farther, 
the  amount  of  suspended  matter  influences 
materially  the  percentage  removal.  The  lat 
ter  point  in  a  measure  follows  from  the  firs^ 
because  when  the  particles  arc  large  the  stage 
of  the  river,  etc..  is  such  that  the  total  weight 
of  the  suspended  matter  is  bound  to  be  great, 
comparatively  speaking.  This  is  shown  by 
the  following  results,  obtained  by  plain  sedi 
mentation  in  one-gallon  bottles. 


Farts  per  Mill! 

pended  Matter 

Percentage  Removal  in     3  h 
"  24 

"48 


of    Original    Sus- 


</>5 
85 
96 


130 
17 
32 
41 


The  above  experiments  show  that,  with 
the  first  water  (Xo.  I),  containing  coarse  and 
heavy  particles,  the  suspended  matters  de 
creased  from  965  to  29  parts;  while  in  the 
third  water  containing  fine  clay  particles,  the 
corresponding  decrease  was  from  130  to  77 
parts.  This  brings  out  the  important  fact 
that  with  the  water  containing  clay  particles, 
such  as  is  found  here  for  two  or  three 
months  in  the  year,  the  removal  of  sus 
pended  matter  is  not  only  much  less  rapid 
than  in  the  water  containing  the  heavier  mud 
and  silt,  but  the  amount  (weight)  of  sus 
pended  matter  at  the  end  of  practicable  lim 
its  of  subsidence  is  greater  in  the  case  of  the 
clay-bearing  water.  In  fact,  with  the  third 
water  it  would  require  weeks,  if  not  months, 
to  remove  from  it  substantially  all  of  the  clay. 
With  the  second  water,  resembling  a  mixture 
of  the  other  two.  the  removal  of  suspended 
matters  was  intermediate  in  its  nature. 

From  the  above  statements  it  will  be  per 
fectly  clear  that  the  efficiency  of  plain  sub 
sidence  depends  very  largely,  so  far  as  any 
given  period  is  concerned,  upon  the  condi 
tions  under  which  subsidence  takes  place.  The 
main  thing  is  to  bring  the  water  into  a  state 
of  comparative  rest,  in  order  to  reduce  the 
vortex  motion  of  the  particles  due  to  eddies 
and  similar  movements  of  the  water.  Ex 
perience  shows  that  the  water  is  brought 
to  a  state  of  rest  much  more  quickly 
in  small  receptacles  than  in  large  reser 
voirs  such  as  would  be  required  in 
practice.  The  results  obtained  from  small 
experimental  devices,  accordingly,  can  be 
taken  only  as  indications  in  general  terms  of 
what  may  be  accomplished  practically  in  this 
manner,  and  as  a  guide  for  the  construction 
of  large  subsiding  basins  might  be  quite  mis 
leading.  Furthermore,  it  was  not  considered 
feasible  during  these  investigations  to  secure 
conditions  on  a  sufficiently  large  scale  to  en 
able  the  efficiency  of  plain  subsidence  on  a 
practical  basis  to  be  studied  in  a  thorough 
manner.  The  following  conclusions  upon  the 
purification  of  the  Ohio  River  water  at  Louis 
ville,  therefore,  are  in  part  presented  in  gen 
eral  rather  than  in  specific  terms. 

Conclusions. 

i.   It  is  possible  to  remove,  economically, 


378 


WATER  PURIFICATION  AT  LOUISVILLE. 


about  75  per  cent,  of  the  suspended  matter 
in  normal  muddy  water  by  plain  sedimenta 
tion  (subsidence).  At  times  of  freshets  dur 
ing  the  winter  and  early  spring  the  percent 
age  might  exceed  90;  while  in  the  late  spring 
and  summer  it  might  fall  to  50  or  less. 

2.  The  removal  of  bacteria  by  plain  sedi 
mentation  follows  the  removal  of  suspended 
matter  in  a  general  way.      But  the  removal 
of  bacteria  by  this  portion  of  an  efficient  sys 
tem  of  purification  is  not  important,  because 
they    can    be   effectively    disposed    of   subse 
quently  by  filtration  without  extra  cost  in  the 
operation  of  the  complete  system,  and  their 
removal    by    the   niters   does    not   affect   the 
quantitative  efficiency  of  nitration,  as  is  the 
case  with  mud  and  other  suspended  matters. 

3.  After  treatment  to  its  economical  limits 
by  plain  sedimentation,  the  Ohio  River  water 
would  ordinarily  be  discolored  by  suspended 
matters,  which  it  would  contain  in  sufficient 
amounts     to     preclude     the     probability     of 
growth  in  the  open  subsidence  basins  of  algae 
and  other  organisms,  giving  rise  to  objection 
able  tastes  and  odors. 

4.  At  times  of  freshets  during  the  spring 
and  summer  all  the  evidence  goes  to  indicate 
that  plain  subsidence  cannot  economically  re 
move  a  sufficient  amount  of  the  fine  clay  car 
ried  in  the  Ohio  River  water  at  Louisville  to 
prepare  the  water  satisfactorily  for  filtration; 
and,   regardless   of  whether  the   English   or 
American  type  of  filter  is  used,  economy  de 
mands  the  use  of  coagulating  treatment  to  aid 
subsidence  at  such  times. 

5.  The  period  of  economical   plain  subsi 
dence  of  the  Ohio  River  water  does  not  ex 
ceed   the   equivalent   of  24   hours'    quiescent 
subsidence,  such  as  is  secured  in  one-gallon 
bottles.      With  the  heavy  coarse  mud  of  the 
winter  freshets  this  period  is  doubtless  shorter 
than  24  hours;    and  in  the  case  of  the  clay- 
bearing  waters,  for  which  the  use  of  coagu 
lants  is  imperative,  the  period  could  to  ad 
vantage  be  somewhat  shorter  than  this.     But 
with  the  intermediate  class  of  water,  resem 
bling  a  mixture  of  these  extremes  and  illus- 
tatecl  by  No.  IT  water  in  the  last  table,  we  are 
led  to  believe  that  plain  quiescent  subsidence 
could  be  economically  carried  to  24  hours,  or 
to  very  nearly  that  period. 

6.  With  regard  to  the  period  of  subsidence, 


under  the  conditions  of  practice,  equiva 
lent  to  24  hours'  quiescent  subsidence  in  one- 
gallon  bottles,  the  available  conditions  of 
these  investigations  were  not  such  as  to  make 
the  solution  of  this  problem  feasible. 

7.  Concerning  the  arrangement  of  the  sub 
sidence  basins,  with  reference  to  size,  depth, 
and  location  of  division  walls;  and  their  op 
eration,  with  regard  to  the  question  of  con 
stant  How,  intermittent  flow,  or  successive 
fillings  and  drawings,  there  are  no  data 
available  from  these  investigations,  and  it  will 
be  necessary  to  rely  upon  information  from 
other  sources. 

SECTION   No.   2. 

ACCOUNT  OF  THE  COMMERCIAL  CHEMICALS 
AVAILABLE  AS  COAGULANTS  FOR  THE 
OHIO  RIVER  WATER  AND  OF  THE 
MANNER  OF  THEIR  BEHAVIOR  WHEN 
APPLIED  TO  THIS  WATER. 

In  this  section  it  is  the  purpose  to  take  the 
entire  list  of  metals  and  show  which  of  them 
form  commercial  compounds  capable  of  co 
agulating  the  Ohio  River  water  in  a  safe 
manner.  The  way  in  which  the  leading 
available  compounds  of  the  suitable  metals 
are  decomposed  when  applied  to  this  water 
is  described,  together  with  the  relative  advan 
tages  and  disadvantages  of  each.  A  fall  de 
scription  of  the  formation  of  coagulating 
chemicals  by  the  electrolytic  decomposition 
of  metal  plates  is  presented  in  sections  Nos. 
3,  4,  and  5.  In  Section  No.  6  the  relative 
efficiency  and  economy  of  the  several  avail 
able  coagulants  is  shown,  and  in  section  No. 
i  5  a  comparison  is  made  of  the  costs  of  the 
chemicals  most  adaptable  for  this  use.  Chap 
ter  III  contains  a  description  of  the  action 
of  sulphate  of  alumina  when  applied  to  the 
Ohio  River  water,  as  far  as  it  was  understood 
in  1896;  and  this  portion  of  the  present 
chapter  is,  in  a  measure,  an  elaboration  of 
Chapter  III,  and  contains  all  of  our  additional 
information  upon  this  subject  at  the  close  of 
these  investigations. 

Classification  of  Afctals  in  their  Applicability  to 
the  Purification  of  the  Ohio  River  Water. 

The  next  table  contains  a  list  of  all  rnetals, 
excepting  the  rare  and  precious  ones,  sub- 


SUMMARY  AND  DISCUSSION   OF   DATA    OF  1807. 


379 


divided  into  groups  according  to  their  gen 
eral  adaptability  for  the  purpose  in  question. 
In  the  first  column  are  given  those  metals 
which  are  either  well-known  poisons,  or 
which  in  small  quantities  are  regarded  in  the 
absence  of  precise  data  as  suspicious  from  a 
hygienic  point  of  view.  The  second  column 
contains  those  metals  the  normal  compounds 
of  which  form  soluble  salts  when  added  to 
this  water;  and  in  the  third  column  are  found 
those  metals  capable  of  forming  in  the  Ohio 
River  water  compounds  of  a  solid  granular 
nature,  wholly  or  partially  insoluble  under  the 
existing  conditions.  In  this  connection  fre 
quent  use  will  be  made  of  "precipitate,"  which 
is  the  chemical  name  for  a  solid  compound. 
Finally,  there  are  presented  in  the  fourth  col 
umn  those  metals  which  form  insoluble  and 
gelatinous  precipitates  when  applied  in  a  suit 
able  manner  to  this  water.  • 

CLASSIFICATION    OF    METALS. 


'     (Division  No.  i. 

Division  No., 

Permissible  Me 

als  from  a  Sani 

ary  Standpoint. 

Group  No    i. 

*•—  »  a  Sanitary 

Group  No.  i  . 

Forming 
Granular 

Group  No.  3. 
Forming 

EB  Standpoint. 

Foi  min^ 
Soluble 
Compounds. 

Precipitates 
Partly  or 
Wholly 

Geh'tinous 
Insoluble 
Precipitates. 

Insoluble. 

Lead 

Sodium 

Calcium 

Aluminum 

Silver 

Potassium 

Magnesium 

Iron 

Mercury 

Manganese 

Tin 

Antimony 

Arsenic 

Copper 

Bismuth 

Cadmium 

Nickel 

Cobalt 

Zinc 

Barium. 

Strontium 

The  metals  of  division  No.  I,  in  the  light  of 
our  present  knowledge,  cannot  be  considered 
as  applicable  for  this  work.  Taking  up  the 
metals  of  division  No.  2,  the  use  of  the  several 
groups  may  be  briefly  outlined  as  follows: 

Group  No.  T. — These  metals  may  be  use:l  in 
the  form  of  hydrate  (caustic  soda)  to  remove 
carbonic  acid  from  water.  This  treatment  pro 
duces  sodium  carbonate  (if  caustic  soda  were 
added),  which  will  decompose  incrusting  con 


stituents  (permanent  hardness).  Sodium  or 
potassium  may  also  be  added  directly  to 
water  in  the  form  of  carbonates  or  tribasic 
phosphates  for  the  purpose  of  removing  in- 
crusting  constituents. 

Group  No.  2. — These  metals  may  be  applied 
to  the  water  in  the  form  of  hydrates  (e.  g.  lime 
water)  in  order  to  remove  carbonic  acid.  From 
such  an  application  there  is  formed  calcium 
carbonate,  which  is  soluble  in  water  free  of 
carbonic  acid,  to  the  extent  of  2  to  3  grains 
per  gallon.  Quantities  in  excess  of  this 
amount  settle  out,  upon  standing,  in  the  form 
of  a  fine  white  powder,  which  has  little  or  no 
power  as  a  coagulant. 

Group  No.  _?. — These  metals  may  be  added 
to  this  water  in  proper  quantities  and  in  a 
suitable  form  with  the  result  that  ultimately 
an  insoluble  gelatinous  precipitate  is  formed, 
capable  of  coagulating  the  suspended  matter. 

The  metals  of  groups  Xos.  i  and  2  refer 
solely  to  metals  for  the  reduction  of  corrod 
ing  and  incrusting  constituents,  and  will  be 
taken  up  subsequently  in  connection  with 
these  matters;  at  present  we  will  consider 
the  metals  of  group  No.  3,  which  are  the  o:ily 
ones  available  for  the  coagulation  of  the 
water,  preparatory  to  subsidence  of  fine  clay 
and  the  rapid  filtration  of  the  water  through 
sand. 

Most  Suitable  Compounds  of  the  Metals  (Group 
No.  3)  capable  of  producing  Coagulating 
Precipitates,  and  a  General  Description  of 
their  Behavior  upon  Application  to  the  Ohio 
River  Water. 

A  comparative  outline  of  the  leading  com 
mercial  compounds  (salts)  of  these  metals  is 
as  follows: 

Compounds  of  Aluminum. 

In  addition  to  sulphate  of  alumina  and  pot 
ash  alum  there  are  several  other  commercial 
compounds  which  have  been  investigated  in 
the  laboratory.  It  was  explained  in  Chap 
ters  II  and  IX  that  the  sulphate  was  the  bet 
ter  of  the  two  former:  and  accordingly  this 
compound  will  be  briefly  described  and  the 
others"  referred  to  it  in  comparative  terms. 

Sulphate  of  Alumina. — The  behavior  of  this 


3  Ho 


WATER    PURIFICATION   AT  LOUISVILLE. 


chemical  when  added  to  the  Ohio  River 
water  has  been  fully  described  in  general 
terms  in  Chapter  111.  As  a  matter  of  con 
venience  it  may  be  repeated  that,  briefly,  it  is 
decomposed  for  the  most  part  by  the  alkaline 
compounds  (lime  and  magnesia)  in  the  river 
water;  and  that  the  increase  in  carbonic  acid 
and  incrusting  constituents  in  the  water  is 
proportional  to  the  decrease  in  alka'inity. 
The  rate  of  decrease  in  alkalinity  (Ci  to  <)  par.s 
per  million  for  j  grain  per  gallon  of  the  or 
dinary  chemical)  depends  upon  the  amount 
of  sulphuric  acid  in  the  chemical  and  the 
amount  of  suspended  matters  in  the  water 
capable  of  absorbing  this  compound.  The 
alumina  in  the  commercial  product  is  pre 
cipitated  and  removed  by  sedimentation  and 
filtration,  while  the  increased  carbonic  add 
and  incrusting  constituents  (principally  sul 
phate  of  lime)  remain  in  the  water.  It  has 
already  been  made  plain  that  the  two  latter 
additions  to  the  water  are  not  desirable  from 
an  industrial  standpoint,  although  they  do 
not  injure  the  sanitary  quality  of  the  water, 
when  the  process  is  carried  on  under  suitable 
conditions.  From  an  economical  point  of 
view  the  amount  of  sulphate  of  alumina 
wasted  by  absorption  by  the  surfaces  of  the 
suspended  particles  of  mud  and  silt,  and  by 
the  organic  matter,  is'  a  matter  of  much  im 
portance.  For  the  sake  of  explicitness  this 
topic  for  all  the  chemicals  is  discussed  by  it- 
se'f  in  this  section  just  after  this  more  general 
account. 

Potash  Alum. — The  crystals  of  this  com 
mercial  chemical  are  a  mixture  of  sulphate  of 
alumina  and  sulphate  of  potash.  The  latter 
portion  is  of  no  practical  influence  in  water 
purification,  while  the  sulphate  of  alumina  in 
it  behaves  in  a  manner  similar  to  commercial 
su'phate  of  alumina  as  described  in  the  last 
paragraph.  Potash  alum  contains  only  about 
two-thirds  as  much  sulphate  of  alumina  as  the 
commercial  form  of  this  last  chemical;  costs 
substantially  the  same;  possesses  no  advan 
tages  in  current  methods  of  use;  and,  there 
fore,  is  eliminated  from  the  problem  on  the 
ground  of  cost. 

Chloride  of  Alumina. — This  compound  be 
haves  in  a  precisely  similar  manner  to  sul- 
nhate  of  alumina  in  forming  a  precipitate  of 
hydrate  of  aluminum  and  reducing  in  the  same 


ratio  the  alkalinity,  with  the  formation  of  car 
bonic  acid  and  incrusting  constituents.  The 
only  difference  is  that  the  increased  amounts 
of  incrusting  constituents  would  be  composed 
of  chlorides  of  lime  and  magnesia  in  place  of 
the  sulphates  of  these  metals.  This  change 
would  produce  only  a  very  slight  and  nomi 
nal  difference  in  the  character  of  the  water, 
because  when  heated  in  a  steam-boiler  under 
pressure  of  50  pounds  the  added  chloride  of 
lime  reacts  with  the  sulphate  of  magnesia 
originally  in  the  water,  and  the  effect  is  simi 
lar  to  the  conditions  when  commercial  sul 
phates  are  applied.  There  probably  would 
not, be  enough  magnesium  sulphate  in  the 
water  to  complete  this  change  at  all  times; 
but  even  in  this  event  it  is  to  be  stated  that 
the  magnesium  chloride  formed  from  this 
chemical  by  the  above  reaction  is  the  com 
pound  which  is  most  injurious  to  boilers,  as  it 
is  decomposed  by  heat  in  boilers  with  the 
formation  of  free  hydrochloric  acid. 

This  chemical  is  more  expensive  than  sul 
phate  of  alumina,  because  the  hydrochloric 
acid  used  in  its  preparation  is  more  costly 
than  sulphuric  acid;  and  as  there  are  no  sub 
stantial  advantages  to  offset  the  increased 
cost  its  use  is  not  practicable. 

Acetate  of  Alumina. — Tn  trade  this  chemical 
is  known  as  "  red-liquor  "  and  is  used  in  dye 
ing.  Tt  is  decomposed  by  the  alkaline  con 
stituents  of  the  river  water  the  same  as  sul 
phate  of  alumina,  with  the  formation  of  alu 
minum  hydrate  and  the  same  rate  of  reduc 
tion  in  alkalinity  and  increase  in  carbonic 
acid.  The  other  resultant  compounds,  ace 
tates  of  lime  and  magnesia,  in  place  of  sul 
phates,  arc  soluble  and  would  appear  in  the 
filtered  water.  They  are  not  injurious  to 
health,  and  do  not  act  as  incrusting  constitu 
ents.  The  absence  of  increased  amounts  of 
the  latter  compounds  would  be  desirable,  but, 
as  the  acetate  costs  about  four  times  as  much 
as  the  sulphate,  the  evidence  in  section  No. 
14  of  this  chapter  shows  that  the  use  of  this 
chemical  would  not  be  advisable. 

Sodium  Alnminatc. — This  compound  of  alu 
minum  differs  essentially  from  sulphate  of 
alumina  in  that  in  this  case  the  aluminum 
ads  as  an  acid  instead  of  a  base.  When  car 
bonic  acid  is  applied  to  sodium  aluminate  so 
lutions  in  certain  industrial  chemical  proc- 


SUMMARY  AND   DISCUSSION   OF  DATA    OF  1897. 


esses  aluminum  hydrate  is  formed  and  so 
dium  carbonate  appears  as  a  by-product.  In 
water  coagulation  such  an  action  would  be 
very  desirable  if  the  conditions  allowed  it  to  be 
have  like  this,  as  the  same  gelatinous  hydrate 
would  be  obtained,  with  no  increase  in  cor 
roding  or  incrusting  constituents;  in  fact  the 
latter  would  be  reduced  because  the  sodium 
of  the  applied  chemical  would  unite  with  car 
bonic  acid  to  form  sodium  carbonate,  which 
in  turn  would  decompose  an  equivalent 
amount  of  incrusting  constituents  without 
forming  any  objectionable  compounds.  In 
other  words,  the  single  compound  would  give 
the  combined  effect  of  the  metals  of  groups 
Xos.  i  and  3  of  division  No.  2  of  the  table. 

Experience,  however,  showed  that  its  use 
was  impracticable  in  the  case  of  the  Ohio 
River  water  because  it  would  not  decompose 
in  the  manner  stated.  The  reason  of  this  ap 
peared  to  be  that  the  solution  in  the  river 
water  of  this  chemical  and  of  carbonic  acid 
was  too  weak. 

Compounds  of  Iron. 

Owing  to  the  fact  that  iron  is  a  cheap 
metal,  and  that  its  hydrate  in  the  oxidized  or 
ferric  state  is  an  excellent  coagulant,  these 
compounds  are  entitled  to  careful  considera 
tion.  At  the  outset  it  is  to  be  recalled  that 
there  are  two  series  of  iron  compounds,  the 
ferrous  (incompletely  oxidized)  and  the  ferric 
(completely  oxidized).  \Ye  shall  first  con 
sider  the  ferrous  compounds. 

I'crrous  Sulphate. — This  is  also  known  as 
the  protosulphate  of  iron  and  as  green  vitriol, 
and  is  the  cheapest  form  in  which  iron  com 
pounds  are  on  the  market.  When  added  to 
the  Ohio  River  water  it  acts  similarly  to  sul 
phate  of  alumina  except  that  ferrous  hydrate 
is  formed  in  place  of  aluminum  hydrate. 
With  equal  weights  of  metal  the  reduction  in 
alkalinity  and  increase  of  carbonic  acid  and 
incrusting  constituents  by  ferrous  sulphate 
and  sulphate  of  alumina  are  in  the  ratio  of 
i.o  to  1.3.  Ferrous  hydrate  is  not  a  suitable 
coagulant  because  it  dissolves  in  the  water 
to  the  extent  of  about  /  parts  per  million: 
and  to  make  the  iron  compounds  available 
it  is  necessary  to  have  the  iron  ultimately  in 
the  form  of  the  ferric  (oxidized)  hydrate.  In 
the  case  of  ferrous  sulphate  there  is  enough 


atmospheric  oxygen  dissolved  in  the  water  to 
accomplish  this  under  favorable  conditions. 
Experience,  however,  shows  that  this  is  im 
practicable  in  this  water,  owing  to  complica 
tions  in  the  oxidation  caused  by  carbonic  acid. 
When  ferrous  sulphate  is  added  to  this  water, 
white  ferrous  hydrate,  mostly  insoluble,  is 
formed.  Very  quickly  this  precipitate  passes 
into  solution,  due  to  the  action  of  carbonic 
acid  and  resulting  probably  in  the  formation 
of  a  soluble  basic  carbonate.  When  the  iron 
is  in  this  form  the  atmospheric  oxygen,  al 
though  present  in  excess,  oxidizes  it  very 
slowly  and  with  great  difficulty.  Further 
more,  the  iron  when  it  does  reach  the  oxi 
dized  state  does  not  form  the  normal  gelat 
inous  ferric  hydrate,  but  a  partially  granular 
compound  which  is  some  lower  hyclration  of 
ferric  oxide  as  nearly  as  could  be  learned. 

In  short,  the  carbonic  acid  in  this  water 
renders  the  use  of  ferrous  sulphate  (and  all 
other  ferrous  compounds)  inadmissible  for 
coagulation,  owing  to  the  passage  of  dis 
solved  iron  through  the  filters.  To  remove 
the  carbonic  acid  before  applying  the  ferrous 
compounds  would  be  too  costly  to  be  prac 
ticable. 

Ferric  Sulphate. — Of  the  commercial  forms 
of  iron  in  the  oxidized  or  ferric  condition, 
ferric  sulphate  or  persulphate  of  iron  is  the 
best  one  for  this  line  of  work  when  economy 
is  considered,  for  the  same  reason  that  the 
sulphate  is  the  best  compound  of  aluminum. 
Ferric  sulphate  is  decomposed  by  the  alka 
line  constituents  of  the  Ohio  River  water  in 
a  manner  precisely  similar,  so  far  as  could  be 
learned,  to  sulphate  of  alumina.  The  result 
ing  precipitate  of  ferric  hydrate  is  very  gelat 
inous  and  is  insoluble:  therefore  it  makes  an 
excellent  coagulant.  With  equal  weights  of 
iron  and  aluminum,  in  the  form  of  sulphates, 
the  ratio  of  the  decrease  in  alkalinity  and  in 
crease  in  carbonic  acid  and  incrusting  con 
stituents  is  i.o  to  2.1.  The  waste  of  ferric 
sulphate  by  absorption  on  the  surfaces  of  silt 
and  mud  is  similar  to  that  in  the  case  of  sul 
phate  of  alumina. 

Commercial  ferric  sulphate  is  a  little 
cheaper  than  sulphate  of  alumina,  free  of 
water  of  crystallization,  and  contains  about 
three  times  as  high  a  percentage  of  metal.  It 
was  these  features  of  the  compound  that 


WATER  PURIFICATION  AT  LOUISVILLE. 


originally  attracted  our  attention.  It  is  diffi 
cult  to  dissolve,  and  the  sample  with  which 
our  tests  were  made  contained  some  free  sul 
phuric  acid  and  insoluble  residue.  Neutra! 
ferric  sulphate  can  be  procured  without  ^ diffi 
culty,  however,  and  the  suspended  particles 
could  be  removed  from  the  solution  by  ready 
means. 

Metallic  Iron  b\  flic  Anderson  Process. — 
This  process  consists  in  obtaining'  in  the 
water  by  contact  with  metallic  iron  a  carbon 
ate  (ferrcr.s)  of  iron  by  the  solvent  action  of 
the  carbonic  acid  in  the  water,  and  the  oxi 
dation  of  this  compound  to  insoluble  ferric 
hydrate.  It  is  referred  to  in  Chapter  IX, 
page  244.  Bottle  experiments  indicated  that 
its  use  with  the  Ohio  River  water  was  not 
satisfactory,  owing  to  the  retarding  action  of 
large  amounts  of  carbonic  acid  such  as  are 
present  for  months  at  a  time  in  this  water. 
The  nature  of  this  retarding  action  is  similar 
to  that  in  the  case  of  the  protosulphate  of 
iron. 

Aeration  was  tried  on  a  small  scale  to  sup 
plement  this  action,  but  it  did  not  work  well. 
The  oxide  was  granular  in  form,  showing  the 
absence  of  normal  hydration,  and  the  value  of 
the  iron  as  a  coagulant  was  lost  for  the  most 
part. 

Compounds  of  Manganese. 

Manganese  forms  manganous,  manganic, 
and  permanganate  compounds.  The  man 
ganous  compounds  cannot  be  safely  used  to 
advantage  with  this  water,  owing  to  compli 
cations  with  carbonic  acid  in  the  manner  ex 
plained  in  the  case  of  ferrous  sulphate. 
Manganic  compounds  in  a  suitable  form  arc 
not  on  the  market.  Permanganates  of  lime 
and  potash  were  used  in  the  laboratory;  they 
are  manufactured  in  considerable  quantities, 
but  they  cost,  according  to  the  best  quota 
tions.  $12.70  and  $0.40  per  pound,  respect 
ively.  Their  expense  renders  their  use  in 
admissible  for  purification  of  municipal  sup 
plies.  A  study  of  them,  however,  has  made 
plainer  our  understanding  of  the  coagulation 
of  the  muddy  Ohio  River  water,  and  for  the 
sake  of  completeness  they  will  receive  brief 
consideration. 

Permanganate  of  Potash. — When  added  to 


the  Ohio  River  water  in  proper  amounts  the 
organic  matter  slowly  withdraws  oxygen 
from  this  compound,  and  the  carbon  and  hy 
drogen  of  the  organic  matter  are  oxidized  to 
carbonic  acid  and  water,  respectively.  The 
result  is  that  after  a  time  the  manganese  is 
converted  to  mangano-manganic  hydrate, 
which  is  a  gelatinous,  insoluble  precipitate. 
Experience  shows  that  the  action  is  very 
slow,  at  least  3  hours  ordinarily  being  re 
quired  for  its  completion;  but  the  time  varies 
with  the  amount  and  character  of  the  organic 
matter.  \Yhen  the  reaction  is  completed  the 
manganese  does  not  pass  through  the  filter, 
but  it  will  do  so  until  it  is  converted  into  the 
insoluble  hydrate.  As  fast  as  the  carbon  di 
oxide  is  formed  it  unites  with  the  potash  of 
the  applied  chemical  to  form  carbonate  of 
potash,  which  is  an  alkaline  but  not  a  corrod 
ing  or  incrusting  constituent.  The  nominal 
increase  in  alkalinity  is  the  only  change  in  the 
composition  of  the  filtered  water,  as  the  re 
moval  of  organic  matter  would  be  effected 
by  subsidence  and  filtration  independent  of 
this  oxidizing  action. 

in  addition  to  the  slowness  with  which  this 
action  takes  place  this  process  developed  an 
important  fact — that  the  manganese  com 
pounds  are  not  at  all  or  very  little  absorbed 
by  the  surface  of  the  mud  or  silt. 

Permanganate  of  Lime. — The 'behavior  of 
this  chemical  when  applied  to  the  Ohio  River 
water  is  precisely  similar  to  that  of  perman 
ganate  of  potash,  except  that  the  resulting 
carbonate  in  this  case  is  that  of  lime  instead 
of  potash. 


Experience  shows  that  the  sulphates  of  alu 
mina  and  ferric  iron  are  the  most  suitable 
commercial  chemicals  for  the  coagulation  of 
the  Ohio  River  water.  In  order  to  make 
more  explicit  the  next  topic,  on  absorption  of 
coagulants  by  silt  and  clay,  the  permanga 
nates  will  be  briefly  reviewed  in  comparison 
with  the  sulphates,  although  the  former  are 
too  expensive  and  are  incapable  of  being  ap 
plied  in  sufficient  amounts  to  be  practicab'e. 
For  convenience  we  will  refer  to  the  sul 
phates  as  type  A,  and  to  the  permanganates 
as  type  B. 


SUMMARY  AND   DISCUSSION   Of  DATA    OF  1897. 


3»3 


/.  Nature  of  Reaction. — This  has  been  care 
fully  explained  above,  but  in  brief  a  type  A 
chemical  is  partly  and  as  a  rule  mostly  de 
composed  by  alkaline  constituents,  while  the 
remainder  is  absorbed  by  the  surface  of  the 
matters  in  suspension.  The  latter  action  ap 
pears-  to  be  largely  if  not  wholly  a  chemical 
one.  With  type  B  the  dissolved  organic 
matter  decomposes  the  chemical,  and  a  re 
sultant  gelatinous  precipitate  is  formed.  So 
far  as  we  could  learn  type  B  appears  to  be 
affected  not  at  all,  practically  speaking,  by 
absorption  by  silt  and  clay,  and  its  reaction 
progresses  with  suspended  organic  matter 
only  so  fast  as  the  latter  becomes  disinte 
grated  and  passes  into  solution. 

2.  Gcrmicidal  Action.  —  The  chemicals  of 
each  type  if  applied  in  sufficiently  large  quan 
tities  will  destroy  bacteria.  But  when  ap 
plied  to  the  water  in  such  amounts  as  are 
practicable  for  the  purification  of  a  municipal 
water  supply  they  do  not  kill  bacteria,  prac 
tically  speaking,  although  they  cause  many  of 
them  to  die  either  by  direct  effect  or  by  en 
veloping  them  in  masses  of  coagula.  In  any 
case  under  practicable  conditions  in  this  con 
nection  the  destruction  of  bacteria  would  not 
be  complete  from  a  hygienic  point  of  view. 

?.  Speed  of  Reaction. — With  type  A  the 
reaction  is  completed  almost  instantaneously, 
although  there  are  indications  that  at  times 
there  is  a  selective  action  in  respect  to  the 
alkaline  constituents  and  the  suspended  par 
ticles  which  absorb  the  chemicals.  Concern 
ing  the  time  which  elapses  before  the  coagula 
appear  in  suitable  size  for  efficient  subsidence 
and  nitration,  this  period  deals  wholly  with 
the  period  of  coagulation  following  the  initial 
reaction,  which  occurs  immediately. 

In  the  case  of  type  B  the  initial  reaction 
takes  place  very  slowly;  in  fact  it  would 
probably  never  be  complete  in  less  than  3 
hours,  and  in  many  instances  it  would  con 
tinue  for  more  than  24  hours.  This  is  due 
to  the  nature  of  the  reaction  as  explained 
above,  as  the  chemical  has  first  to  disinte 
grate  and  make  soluble  a  large  part  of  the 
organic  matter  which  is  oxidized. 

4.  Safe  Maximum  Limit  of  Application. — 
The  maximum  limit  of  safe  application  of 
type  A  depends  upon  the  absorptive  capac 
ity  of  suspended  matters,  and  the  alkalinity 


of  the  river  water,  and  the  amount  of  sul 
phuric  acid  in  the  applied  chemicals.  Ex 
pressed  in  grains  per  gallon  the  range  of 
maximum  application  of  sulphate  of  alumina 
would  be  from  4  to  15.  For  persulphate  of 
iron  these  figures  would  range  approximately 
from  3  to  10  grains  per  gallon. 

In  the  case  of  permanganate  of  potash, 
type  B,  the  safe  maximum  application  would 
range  from  o.  i  to  0.2  grain  per  gallon,  with 
a  period  of  reaction  of  not  less  than  3  hours. 

5.  Applicability  in  the  Purification  of  the 
Ohio  River  Water.  —  The  permanganates, 
type  B.  are  not  applicable  to  this  problem 
because  of  their  cost,  the  slowness  of  their 
action,  and  the  low  limits  in  the  amount  of 
safe  application.  A  study  of  them,  however, 
was  very  fruitful  in  showing  inherent  weak 
ness  of  type  A  chemicals,  and  indicating  how 
those  weaknesses  might  be  remedied  in  part 
in  practice.  They  relate  to  absorption  and 
are  discussed  as  the  next  topic. 

ABSORPTION  OF  COMMERCIAL  SULPHATES 
OF  ALUMINA  AND  OF  FERRIC  IRON  BY 
THE  SILT  AND  CLAY  IN  THE  OHIO 
RIVER  WATER,  WITH  SPECIAL  REFER 
ENCE  TO  THE  WASTE  OF  CHEMICALS 
AND  THE  NECESSITY  FOR  THE  REMOVAL 
OF  COARSE  SILT  BY  PLAIN  SEDIMENTA 
TION. 

In  the  course  of  these  investigations  a 
number  of  observations  were  made  which  co 
operated  to  bring  out  the  marked  significance 
from  a  practical  point  of  view,  of  a  phenome 
non  which  we  shall  call  absorption.  To  illus 
trate  this  by  an  action  which  is  familiar  to 
everyone,  we  may  compare  it  to  the  some 
what  similar  observation  of  iron  stains  as 
they  appear  upon  linen.  This  action  is  not 
the  same,  but  it  is  believed  that  its  nature  is 
parallel.  At  this  point  it  may  be  stated  that 
of  all  the  chemical  actions  seen  in  daily  life, 
there  is  probably  none  which  is  more  obscure 
than  the  action  of  liquids  upon  solids,  as  illus 
trated  by  the  ones  in  question..  To  explain 
these  observations  and  facts  in  a  comprehen 
sive  manner  is  impossible  in  the  present  state 
of  applied  chemical  science.  Accordingly  we 
shall  present  the  evidence  in  a  series  of  ob 
servations  characteristic  of  the  nature  of  this 


WATER   PURIFICATION  AT  LOUISVILLE. 


phenomenon,  and  at  the  close  point  out  its 
practical  significance. 


This  is  shown  by  the  following  experiment, 
in  which  a  series  of  one-gallon  bottles  were 
filled  with  river  water  containing  424  parts 
per  million  of  mixed  coarse  and  fine  silt  and 
clay.  Beginning  with  none,  the  samples  were 
treated  with  sulphate  of  alumina,  each  bottle 
being  given  0.25  grain  per  gallon  more  than 
the  preceding  one.  The  bottles  were  then 
well  shaken,  and  samples  of  the  supernatant 
liquid  removed  by  a  siphon  after  24  hours 
subsidence.  The  results  were  as  follows: 


After  Settli 

g  24  Hours. 

Additional 

°Grain™per' 

Gallon. 

Suspended 
Solids. 
Parts  per 
Million. 

Percentage 

Removal. 

Portions  of 
o.,5  Grain. 

None 

o.  25 

47 

74 

4 

o.  50 

44 

76 

2 

0-75 

35 

Si 

5 

I.OO 

3 

97 

1  6 

1.25 

i 

99 

2 

1.50 

o 

IOO 

I 

This  experiment  is  not  an  extreme  case, 
but  it  serves  to  illustrate  the  fact  that  with 
successive  equal  amounts  of  applied  sulphate 
of  alumina  the  work  accomplished  is  not 
regularly  progressive,  and  that  for  some  rea 
son  in  the  ordinary  river  water  the  specific 
efficiency  of  the  first  portion  of  chemicals  is 
very  low,  and  less  than  that  of  subsequent 
ones. 


II. 


Necessity  of  Applying  Different  Amounts  of 
Coagulants  to  secure  complete  Coagulation 
of  Equal  Weights  of  Suspended  Matters  of 
Different  Character. 

This  was  repeatedly  noted  in  the  operation 
of  the  filter,  but  is  illustrated  in  a  very  charac 
teristic  manner  by  the  following  experiment: 


Waters  A  and  B  each  contained  66  parts 
per  million  of  suspended  matter.  A  repre 
sents  unusually  fine  particles,  while  in  B  the 
particles  were  abnormally  coarse.  As  in  the 
foregoing  experiment,  successive  portions  of 
sulphate  of  alumina  were  added  to  a  series  of 
bottles  containing  the  two  waters,  respect 
ively,  and  samples  of  the  supernatant  liquid 
were  collected  for  analysis  after  the  coagu 
lant  and  water  had  been  shaken  and  then  al 
lowed  to  subside  for  18  hours. 


After  Settlir 

g  !8  Hours. 

Applied 
Sulphate- 

Wat 

-T   A. 

Wat 

er  B. 

Grains  per 
Gallon. 

Percentage 
Removal  of 
Suspended 
Solids. 

Additional 
Removal  for 

Removal** 

Suspended 
Solids. 

Additional 
Removal  for 

0.25  Grain. 

0.25 

10 

O 

57 

7 

0.50 

10 

O 

72 

15 

0.75 

15 

5 

92 

20 

I.OO 

30 

ic 

96 

4 

1.50 

82 

52* 

99 

3* 

2.UO 

92 

10* 

TOO 

i* 

*  For  increases  of  0.50  grain. 

These  results  show  that  0.75  grain  effected 
as  much  purification  by  coagulation  and  sub 
sidence  with  the  water  B,  containing  the 
coarse  matters,  as  did  2.00  grains  in  the  case 
of  the  water  A,  with  very  fine  clay.  With 
water  A  the  first  point  in  this  evidence  is 
brought  out  very  forcibly,  as  0.5  grain  was 
applied  with  no  purification  in  addition  to 
that  accomplished  by  plain  subsidence. 


III. 

retrying  Departures  from  the  Theoretical  Rate 
of  Reduction  in  Alkalinity  when  Coagu 
lants  are  applied  to  Water  containing 
Equal  Amounts  of  Different  Kinds  of 
Suspended  Matter. 

Tn  Chapter  III  it  was  shown  that  theoretic 
ally  the  reduction  in  alkalinity  would  be 
strictly  proportional  to  the  amount  of  chem 
ical  added  and  to  the  percentage  of  sulphuric 
acid  contained  in  the  applied  sulphate,  pro 
vided  there  were  no  organic  or  suspended 


SUMMARY  AND   DISCUSSION   OF  DATA    Of    1897. 


3*5 


matters  present.  Data  were  presented  a* 
that  time  showing  that  the  departure  from 
the  theoretical  reduction  was  dependent 
upon  the  amount  of  suspended  matter;  and 
here  it  is  the  purpose  to  show  that  the  reduc 
tion  is  also  affected  by  the  character  of  the 
suspended  matter. 

The  following  experiment  illustrates  this 
point.  The  five  samples  of  river  water  con 
tained  approximately  equal  amounts  of  sus 
pended  matter,  while  the  actual  reduction  in 
alkalinity  by  adequate  amounts  of  the  same 
lot  of  sulphate  of  alumina  showed  wide  varia 
tions  in  departure  from  the  theoretical  reduc 
tion. 


These  data  show  clearly  that  different 
kinds  of  suspended  matter  dispose  of  vary 
ing  amounts  of  coagulant  by  an  action  which 
for  the  want  of  a  better  name  we  call  ab 
sorption.  This  is  most  marked  in  the  case 
of  clay,  and  appears  to  be  largely,  if  not 
wholly,  a  chemical  action.  The  reason  of 
this  belief  is  based  on  the  fact  that  there  is  no 
diminution  in  the  conductivity  of  a  solution 
in  which  absorption  takes  place,  and  the  as 
sumption  that  this  indicates  the  absence  of  a 
physical  change  which  would  withdraw  and 
not  interchange  ions  and  thus  increase  the 
resistance  of  the  solution  containing  these 
particles. 

The  absorption  of  chemical  solutions  by 
various  materials  containing  alumina  has 
been  known  for  some  time  to  agricultural 
chemists,  and  at  the  Lawrence  Experiment 
Station  this  action  was  found  to  be  a  factor 
in  connection  with  the  efficiency  of  filters  of 
the  English  type.  In  the  case  of  clay  this 
absorption,  it  is  important  to  note,  produces 
some  coagulation.  \Yith  regard  to  the  co 
agulation  of  clay  by  other  salts,  such  as  com 
mon  table  salt,  or  by  acids,  so  far  as  our  ob 
servations  go,  there  would  be  nothing  prac 
ticable  in  their  use. 


—•  '"— 

Suspended  Solids. 
Parts  per  Million. 

Percentage  whicli  the  Actual 
Reduction  in  Alkalinity  was 
of  the  Theoretical. 

I 

500 

57 

2 

534 

74 

3 

534 

77 

4 

516 

80 

5 

558 

84 

Averages 

550 

74 

IV. 

Conclusive  Indications  of  the  Necessity  of  hav 
ing  to  Saturate  some  Capacity  of  the 
Suspended  Particles  before  complete  Co 
agulation  is  possible. 

The  foregoing  data  bring  out  very  forcibly 
the  fact  that  with  ordinary  conditions  of  the 
river  water  the  first  portions  of  the  coagulant 
have  a  very  low  specific  efficiency  in  purifica 
tion;  and  after  a  certain  amount  has  been 
applied  a  very  small  additional  amount  causes 
complete  coagulation,  provided  sufficient 
time  is  allowed  to  elapse  after  the  applica 
tion  of  the  coagulant.  This  capacity  is  the 
absorption  previously  referred  to.  and  varies 
materially  with  different  waters. 


V. 


Comparison  of  flic  Relative  Efficiencies  as  Sub 
siding  Coagulants,  of  Type  A  (sulphates) 
and  Type  B  (permanganates),  and  with 
Reference  to  Discrepancies  between  the 
above  Relation  and  tim  Percentages  which 
the  Actual  were  of  the  Theoretical  Reduc 
tion  in  Alkalinity. 

At  the  outset  it  may  be  stated  that  in  gen 
eral  terms  experience  indicates  that  to  secure 
equal  efficiencies  for  coagulation,  it  is  neces 
sary  to  provide  substantially  equal  volumes  of 
gelatinous  hydrate.  This  is  demonstrated  by 
the-  data  given  in  section  Xo.  6,  but  here  it 
may  be  noted  that  ordinary  commercial  sul 
phate  of  alumina  and  persulphate  of  iron 
yield  about  the  same  volume  of  hydrate,  and 
as  coagulants  their  efficiency  is  substantially 
the  same  in  all  conditions  which  we  have 
studied. 

On  the  basis  of  equal  volumes  of  hydrate, 
sulphate  of  alumina  and  permanganate  of 
potash  should  have  relative  efficiencies  of  i.oo 
to  1.14.  In  practice  with  the  unsubsided 
Ohio  River  water  the  relative  efficiency  of 
sulphate  of  alumina  was  far  less  than  this,  as 
is  indicated  by  the  following  representative 
results  obtained  from  a  series  of  experiments, 
in  which  in  all  cases  coagulants  were  added  to 
give  a  fairly  complete  and  corresponding  de 
gree  of  efficiency,  as  shown  by  the  removal  of 


WATER   PURIFICATION  AT  LOUISVILLE. 


suspended  matters  by  subsidence  for  24  hours. 
The  comparative  efficiencies  of  types  A  and 
B  are  expressed  with  reference  to  the  above 
ratio. 


Type  A. 


I.  00 

2.OO 


I.  00 
I.  00 


0.10 
O.2O 

o  14 

0.14 

I.  00* 


PercentHge 

.Pcrcen'ta^e 

which  the 

which  the      '. 

spended 

Actual 

Efficiency  of 

olids. 

Reduction  of 

Tvpe  A  was  of 

rts  per 

Alkalinity 

that  indicated 

illinn. 

was  of  the 

by  the 
Theoretical 

Type  A. 

Ratio. 

542 

58 

15 

542 

64 

14 

129 

89 

13 

S3 

91 

-4 

200 

95 

127"- 

*  In  this  case  an  excess  of  dissolved  organic  matter 
was  applied  to  the  water  so  as  to  increase  very  largely 
the  speed  of  reaction. 

Bearing  in  mind  the  fact  that  with  type  A 
the  reaction  is  practically  instantaneous,  while 
in  type  P»  it  is  exceedingly  slow,  with  river 
water,  it  will  be  understood  that  the  coagu 
lating  hydrate  in  type  A  is  formed  very 
quickly  and  in  type  B  very  slowly.  It  is  also 
to  be  remembered  that  type  A,  but  not  type 
I!,  is  absorbed  by  suspended  matter. 

If  the  absorption  were  the  only  point  of 
difference  in  the  behavior  of  the  two  types 
then  the  percentage  efficiency  which  type  A 
gave  of  that  indicated  by  the  theoretical  ratio 
would  correspond  to  the  percentage  which 
the  actual  was  of  the  theoretical  rate  of  re 
duction  of  alkalinity  in  a  general  way.  If  the 
absorption  produced  no  coagulation  of  clay 
particles  this  last  statement  would  be  true  in 
absolute  terms.  But  it  is  shown  in  the  last 
table  that  in  the  case  of  the  first  four  (normal) 
waters  the  percentage  efficiency  of  type  A 
fell  far  below  the  percentage  which  the  actual 
reduction  in  alkalinity  was  of  the  theoretical. 
In  other  words,  the  amount  of  aluminum  hy 
drate,  which  was  proven  to  be  formed  by  the 
actual  decomposition  of  alkaline  constituents, 
failed  to  accomplish  as  much  work  as  an 
equal  volume  of  hydrate  of  manganese  as  pro 
duced  by  type  B. 

The  explanation  of  these  results,  and  of 
others  of  a  similar  nature,  was  that  the  hy 
drate  with  type  A  was  formed  instantane 
ously,  or  nearly  so,  and  became  attached  by 
some  means  to  the  coarse  particles,  which  sub 
sided  quickly  and  carried  to  the  bottom  much 
of  the  hydrate  before  it  had  an  opportunity 


to  coagulate  those  fine  particles  which  needed 
it  most.  This  explanation  was  proved  con 
clusively  to  be  correct  by  adding  enough 
soluble  organic  matter  to  the  last  water  in 
the  case  of  type  B  to  form  this  hydrate  almost 
immediately,  as  was  normally  the  case  with 
type  A.  Under  these  circumstances  the 
relative  efficiency  of  type  A  as  compared 
with  type  B  exceeded  the  theoretical  ratio 
stated  above,  which  was  based  on  the  rela 
tive  volumes  of  hydrate. 

It  is  now  seen  that  in  addition  to  the  ab 
sorptive  action  which  with  coarse  matters 
means  a  waste  of  chemicals,  there  is  also 
an  attachment  of  hydrate,  in  the  case  of  sul 
phate  of  alumina  and  persulphate  of  iron,  and 
the  coarse  particles,  on  which  this  attachment 
occurs,  subside  quickly  and  thus  cause  a 
waste  of  coagulants.  Whether  or  not  this  at 
tachment  is  entirely  physical  or  mechanical 
in  its  nature  is  not  known. 

Conclusions. 

1.  The    suspended    matters    in    the    Ohio 
River    water    have    a    certain,    but    varying, 
power  of  absorbing  sulphate  of  alumina  and 
persulphate  of  iron.     With  fine  clay  particles 
this    absorption    produces    coagulation    in    a 
measure,  but  with  the  coarsest  particles  it  ap 
pears  to  be  a  total  loss  of  chemicals.      This 
absorption  of  the  coagulant  causes  the  actual 
rate  of  reduction  of  alkalinity  to  become  va 
riable,  and  the  departure  from  the  theoretical 
rate  measures  the  absorption  of  the  applied 
chemicals  by  the  suspended  (and  soluble  or 
ganic)  matters. 

2.  In  order  to  secure  complete  coagulation 
for   any    given    water    containing   suspended 
matter  it  is  necessary  to  apply  a  certain  defi 
nite  amount  of  the  coagulant,  which  varies 
with    different    kinds    and    amounts    of    sus 
pended  matter,  in  order  to  saturate  their  ab 
sorptive  power  before  substantial  coagula'ion 
takes  place.     When  applied  in  amounts  less 
than  this  the  chemicals  are  largely  wasted. 

3.  Owing  to  the  fact  that  with  the  com 
mercial  sulphates  the  respective  hydrates  are 
formed  almost  instantaneously,  the  presence 
of    coarse    particles    which    subside    quickly 
cause  a  waste  of  chemicals  in  amounts  equal 
to    the    quantities    of    original    chemical    ab- 


SUMMAA'Y  AND  DISCUSSION  OF  DATA    OF  18<>7. 


sorbed,  plus  a  certain  amount  of  hydrate 
which  becomes  attached  to  their  surfaces. 
The  attached  hydrate  is  thus  removed  before 
it  coagulates  to  its  full  power  the  fine  par 
ticles  in  the  water. 

4.  The  above  facts  are  decisive  proof  that 
it  is  impracticable  to  apply  coagulants  to  a 
water  which  contains  suspended  matter 
which  may  be  economically  removed  by  plain 
subsidence. 

For  the  sake  of  completeness  it  may  be 
stated  that  in  the  electrolytical  formation  of 
coagulating  hydrates  the  salts  of  the  metals 
are  formed  initially,  and  the  general  effect  is 
similar  to  that  recorded  for  the  sulphates  in 
this  section.  So  far  as  our  observations  ex 
tend  at  present,  plain  subsidence  is  the  only 
practical  step  to  take  to  obviate  these  actions 
in  part. 


SECTION   No.   3. 

STATUS  AT  THE  BEGINNING  OF  THIS  POR 
TION  OF  THE  INVESTIGATION,  WITH  A 
GENERAL  DESCRIPTION,  OF  THE  FORMA 
TION  OF  COAGULATING  CHEMICALS  BY 
THE  ELECTROLYTICAL  DECOMPOSITION 
OE  METAL  PLATES. 

At  the  outset  of  this  portion  of  the  investi 
gation  the  evidence  upon  this  point  may  be 
briefly  outlined  as  follows: 

1.  Copper,  lead,  tin,  and  zinc  are  inadmis 
sible   for  electrolytic   decomposition   for  this 
purpose,  because  the  resultant  chemicals  are 
partially  soluble  in  water,  and  would  there 
fore  be  liable  to  injure  the  health  of  persons 
drinking  the  water  after  such  treatment. 

2.  Aluminum  and  iron  are  the  only  metals 
of  commerce  which  can  be  electrolytically  de 
composed  into  chemicals  adapted  to  the  co 
agulation  of  water.     The  available  informa 
tion   concerning   them   at   that    time  was   as 
follows: 

3.  One  pound  of  metallic  aluminum,  elec 
trolytically   decomposed    into   aluminum    hy 
drate,  is  substantially  equivalent  to  one  pound 
of  aluminum  in  the  form  of  aluminum  sul 
phate,  when  the  latter  is  applied  to  a  water 
containing  lime  in  solution.     One  pound  of 


[  metallic  aluminum  in  sheet  form  costs  27 
cents,  and  one  pound  of  aluminum  in  the 
form  of  sulphate  of  alumina  costs  16  cents. 
The  alumina  in  the  form  of  the  commercial 
chemical,  therefore,  costs  only  60  per  cent,  as 
much  as  in  the  form  of  metal  plates,  dis- 

I  regarding  the  expensive  items  of  power,  elec 
trolytic  cells,  and  waste  of  metal  in  the  latter 
case. 

4.  One  pound  of  metallic  iron  electrolytic- 
ally  decomposed  into  iron  hydrate  is  substan- 

i  tially  equivalent  to  one  pound  of  iron  in  the 
form  of  persulphate  of  iron,  when  the  latter 

:  is  applied  to  water  containing  lime  in  solu 
tion.  One  pound  of  metallic  iron,  in  the 
form  of  plates  suitably  arranged  in  an  elec 
trolytical  cell,  costs  about  2  cents;  and  one 
pound  of  iron  in  the  form  of  persulphate  of 
iron  costs  5  cents.  There  was  a  difference, 
therefore,  of  3  cents  per  pound,  to  cover  the 
cost  of  electric  power  and  waste  of  metal. 
This  was  a  substantial  margin  on  the  right 
side,  and  made  the  electrolytic  production  of 
iron  hydrate  a  factor  in  the  problem. 

5.  Electrolytically    produced   hydrates    fei- 
ther   aluminum   or  iron)   do   not,   as   in   the 
case   of   commercial   chemicals   like   the   sul 
phates,  add  to  the  water  a  strong  acid,  to 
combine  with  lime  and  increase  the  incrust- 
ing  power  of  the  water  when  used  in  steam- 
boilers;    nor  is  there  a  practically  equivalent 
amount  of  carbonic  acid  gas  liberated,  to  in 
crease    the    corrosive    action    of   the    filtered 
water  on  iron  vessels. 

In  short,  it  will  be  seen  that  the  electro 
lytic  production  of  iron  hydrate  was  a  promis 
ing  factor,  while  the  electrolytic  production 
of  aluminum  hydrate  gave  no  indications  of 
being  practicable  for  regular  use,  owing  to 

j  excessive  cost.  It  was  decided,  however,  to 
investigate  the  electrolytic  production  of  the 
hydrates  of  both  of  these  metals.  In  the  case 
of  aluminum  this  was  done,  not  only  for  the 
purpose  of  securing  comparable  data  on  the 
same  scale  as  was  used  in  1895-96,  but  also 
with  the  possibility  in  mind  that  the  use  of 
aluminum  during  periods  of  maximum  treat 
ment  of  the  water  might  reduce  the  size  of 
power  plant,  because  it  appeared  that  alu 
minum  is  decomposed  with  less  power  than 
iron,  relatively  speaking. 

I       A  description  of  the  formation  of  iron  by- 


\VATER    PURIFICATION  AT  LOUISVILLE. 


drate  and  of  aluminum  hydrate,  by  the  elec 
trolytic  decomposition  of  the  respective  met 
als,  is  presented  in  considerable  detail,  from  a 
practical  point  of  view,  in  the  next  two  sec 
tions.  Before  this  is  clone,  however,  it  will 
be  well  to  consider  some  of  the  general  fea 
tures  of  electrolvsis. 


Electrolysis  is  the  name  of  the  process  by 
which  a  liquid  is  decomposed  by  means  of 
an  electric  current.  As  a  rule,  such  liquids 
are  aqueous  solutions  of  various  chemical 
salts  and  compounds  which  are  capable  of 
splitting  (dissociating)  into  two  component 
parts.  Liquids  which  can  be  electrolyzed  are 
called  electrolytes.  Absolutely  pure  water 
cannot  be  electrolyzed,  practically  speaking, 
and  liquids  possess  this  capacity  by  virtue  of 
the  chemical  compounds  dissolved  in  them. 
These  compounds  serve  as  conductors  of  the 
electrical  current,  and  electrolytes  are  called 
conductors  of  the  second  class,  in  distinction 
from  the  metals,  which  are  known  as  con 
ductors  of  the  first  class. 

A  receptacle  in  which  electrolysis  takes 
place  is  called  an  electrolytic  cell.  The  plates 
attached  to  the  ends  of  the  wires  running 
from  the  electric  generator  to  the  cell  and 
return  are  spoken  of  as  the  electrodes.  To 
distinguish  the  two  plates,  or  two  sets  of 
plates,  the  electrode  by  which  the  electric 
current  enters  is  termed  the  positive  pole,  or 
anode,  and  that  by  which  it  leaves,  the  nega 
tive  pole,  or  cathode.  The  dissolved  chem 
icals  in  the  water  are  dissociated  into  two 
component  parts,  which  are  called  ions. 
When  an  electric  current  is  passed  through 
an  electrolytic  cell  the  ions  move  to  the 
electrodes.  The  metallic  (including  hydro 
gen)  constituents  or  ions  of  the  substances 
dissolved  in  the  water  pass  to  the  cathode  or 
negative  pole,  while  the  acid  ions  move  to  the 
anode.  The  former  ions  are  called  cathions, 
and  the  latter  anions.  This  movement  to 
ward  the  respective  electrodes,  of  the  metallic 
and  acid  portions  of  the  compounds  dissolved 
in  the  liquid,  explains  the  manner  in  which  an 
electric  current  is  conducted  through  ordi- 
narv  water.  Having  made  this  point  clear,  we 


will  now  proceed  to  consider  the  most  impor 
tant  point  in  question,  viz.:  the  action  of  the 
ions  when  they  reach  electrodes  of  different 
composition. 

Electrodes  may  be  divided  into  two  classes, 
according  to  their  ability  or  non-ability  to  be 
dissolved  by  the  ions  which  reach  the  positive 
pole,  with  the  formation  of  new  chemical 
compounds.  Some  electrodes,  such  as  car 
bon  and  platinum,  are  not  dissolved  by  the 
anions,  which  find  it  easier  to  attack  water 
and  decompose  it.  Such  electrodes  are 
called  passive  or  insoluble.  Other  electrodes, 
such  as  aluminum  and  iron,  form  new  chem 
ical  compounds  by  the  solvent  action  of  the 
anions,  which  find  it  easier,  wholly  or  in  part, 
to  unite  with  the  metal  electrodes  than  to  at 
tack  and  decompose  water.  Such  electrodes 
are  called  active  or  soluble.  Of  the  two  ex 
pressions,  passivity  and  solubility  of  elec 
trodes,  the  former  is  preferred,  and  hereafter 
we  shall  use  it  exclusively.  As  implied  above, 
all  negative  poles,  regardless  of  their  compo 
sition,  are  considered  to  be  passive. 

I'assii'c  Electrodes. — When  carbon  or  other 
passive  electrodes  are  employed  in  the  elec 
trolysis  of  a  liquid  there  are  no  new 
chemical  compounds  permanently  formed, 
but  the  water  is  gradually  decomposed  into 
its  constituent  parts,  hydrogen  and  oxygen 
gases.  To  illustrate  this  we  will  consider  the 
electrolysis  with  carbon  electrodes  of  a  solu 
tion  of  common  salt,  sodium  chloride,  in  pure 
water.  The  chemical  symbol  of  salt  is  Na  Cl, 
in  which  Xa  refers  to  sodium  and  Cl  to 
chlorine. 

When  an  electric  current  is  applied  to  an 
electrolytic  cell  in  which  the  electrolyte  is  a 
salt  solution  the  united  action  is  as  follows: 

Before  Application  of  the  Current. 


Salt  Solution. 

NaCl   NaCl  NaCl  NaCl  NaCl 
NaCl     NaCl     NaCl     NaCl 


SUMMARY  AND   DISCUSSION   OF  DATA    OF  18!>7. 


3«9 


After  Application  of  the  Current. 


Cl    Cl    Cl    Cl    Cl    Cl    Cl 
Na  Na  Na  Na  Na  Na  Na 


That  is,  the  electric  current  is  conducted 
through  the  liquid  by  the  passage  of  the  so 
dium  and  chlorine  ions  to  the  negative  and 
positive  poles,  respectively.  When  the  ions 
reach  the  electrodes  their  electric  charges  are 
neutralized,  and  they  find  in  each  case  that 
the  carbon  poles  are  passive  and  do  not  offer 
any  opportunity  for  chemical  combination. 

Under  these  circumstances  the  second  step 
in  the  process  consists  of  the  ions  at  each  elec 
trode  attacking  water.  At  the  positive  pole 
the  chlorine  ions  unite  with  water  and  form 
hydrochloric  acid  (HC1),  which  remains  dis 
solved  in  the  water,  and  oxygen  (O),  which 
escapes  as  a  gas.  The  sodium  ions  at  the 
negative  pole  also  unite  with  water  and  form 
sodium  hydrate  (NaOH),  commonly  called 
caustic  soda,  which  remains  dissolved  in  the 
water,  and  hydrogen  (H),  which  escapes  as 
a  gas.  This  second  step  in  the  process  may 
be  illustrated  as  follows: 


e 
. 

0  (gas)                             (gas)  H 

. 
_ 

HC1                                NaOH 

Cl     Cl     Cl             Na     Na     Na 

If  a  porous  (parchment)  partition  were 
placed  in  the  cell  between  the  electrodes,  it 
would  be  found  that  the  water  in  the  vicinity 
of  the  positive  electrode  becomes  more  and 
more  acid  as  the  passage  of  the  electric  cur 
rent  continues,  and  the  water  in  the  vicinity 
of  the  negative  electrode  becomes  corre 
spondingly  alkaline.  Hydrochloric  acid  and 


sodium  hydrate  have  a  strong  affinity  for  each 
other,  and  in  the  absence  of  a  partition  unite 
and  form  salt,  the  substance  which  was 
started  with,  and  water.  This  combination 
of  two  of  the  intermediate  products  to  form 
the  original  product  constitutes  the  third  and 
last  step  of  the  process. 


O  (gas)  (gas)  H 

NaCl 
11C1  NuOII 

1 1 .0 
Cl    Cl    Cl  Na  Na  Na  Na 


It  will  thus  be  seen  that  with  passive  elec 
trodes,  electrolysis  of  salt  solution  effects  in 
directly  the  separation  of  water  into  its  com 
ponent  elements,  and  that  by  a  recombination 
of  other  secondary  products  the  original  sub 
stance  is  produced,  and  the  process  is  there 
fore  continuous. 

Active  Electrodes. — In  order  to  make  this 
parallel  with  the  preceding  account  of  pas 
sive  electrodes  we  will  consider  the  e'ec- 
trolysis  of  a  salt  solution  when  the  electrodes 
are  of  iron.  Here  the  first  step  in  the  process, 
the  conduction  of  the  electric  current  by  the 
movement  of  the  chlorine  and  sodium  ions  to 
the  positive  and  negative  poles,  respectively, 
is  precisely  the  same  as  in  the  foregoing  de 
scription. 

With  regard  to  the  second  step  in  the  proc 
ess,  the  action  of  the  sodium  ions  at  the  nega 
tive  pole  is  also  the  same  (because  all 
negative  poles  are  theoretically  passive),  at 
tacking  water  with  the  formation  of  sodium 
hydrate  and  hydrogen  gas.  The  action  of 
the  chlorine  ions  at  the  positive  pole  shows 
the  difference  between  carbon  and  iron  elec 
trodes.  In  this  latter  case  it  is  easier  for  the 
chlorine  to  dissolve  the  iron  electrodes  than 
to  attack  water.  Under  the  most  favorab'e 
conditions  iron  chloride  is  formed  without 
any  oxygen,  and  under  ordinary  circum 
stances  the  amount  of  oxygen  formed  ap 
pears  to  be  very  small,  and  perhaps  nil. 

The  third  step,  the  combination  of  iron 
chloride  and  sodium  hydrate  to  form  sodium 


39° 


WATER   PURIFICATION   AT  LOUISVILLE. 


chloride  (the  initial  compound)  and  iron  hy 
drate,  is  precisely  similar  to  the  correspond 
ing;  step  in  the  case  of  passive  electrodes. 
The  only  difference  in  this  particular  is  that 
iron  hydrate  instead  of  water  (which  may  be 
regarded  as  hydrogen  hydrate)  is  formed. 

From  the  above  description  it  will  be  seen 
that  the  activity  of  iron  and  aluminum  elec 
trodes  u:akes  their  use  possible  as  a  means  of 
producing  hydrates  of  these  metals.  The  de 
gree  of  passivity,  even  of  the  same  metal, 
with  different  salts  dissolved  in  the  water  va 
ries  widc'v  under  the  conditions  of  practice. 
A  consideration  of  this,  and  several  other  im 
portant  factors,  in  the  electrolytic  production 
of  iron  hydrate  and  aluminum  hydrate,  is 
taken  up  in  the  next  two  sections,  in  which 
the  matter  is  described  in  detail  from  a  prac 
tical  point  of  view. 

Fundamental  Lat^s  and  Principles  of  Electrol 
ysis,  as  Applied  to  the  Electrolytic  forma 
tion  of  Hydrates  of  Iron  and  Aluminum 
in  the  Ohio  River  U'atcr. 

The  leading  laws  and  principles  dealt  with 
in  this  work  are  as  follows: 

/.  Faraday's  Quantitative  Law. — This  law 
may  be  expressed  in  a  number  of  different 
ways,  among  which  is  the  following:  The 
amount  of  an  ion  liberated  at  an  electrode 
in  a  given  length  of  time  is  equal  to  the 
strength  (amperage)  of  the  electric  current, 
multiplied  by  the  electro-chemical  equivalent 
of  the  ion.  The  electro-chemical  equivalent 
of  hydrogen  for  one  ampere  of  current  for 
one  hour  is  equal  to  0.375  gram  (5.78 
grains).  On  this  basis  the  electro-chemical 
equivalent  of  any  ion  may  be  obtained  by 
multiplying  the  above  figures  by  the  chem 
ical  equivalent  weight  of  the  ion.  In  the  case 
of  elementary  ions,  this  chemical  equivalent 
weight  is  the  atomic  weight  divided  by  the 
valency,  and  in  the  case  of  compound  ions,  it 
is  the  molecular  weight  divided  by  the  va 
lency. 

From  Faraday's  law  it  follows  that,  other 
conditions  being  equal,  the  amount  of  hy 
drate  of  iron  or  aluminum  formed  is  propor 
tional  to  the  amperage  of  the  current;  and 
the  amount  of  coagulating  chemicals  is  there 
fore  controlled  by  regulating  the  amperage  of 
the  current. 


2.  Ohm's  Law. — Ohm's  law,  that  the  num 
ber  of  amperes  of  current  flowing  through  a 
circuit  is  equal  to  the  number  of  volts  of  elec 
tro-motive  force,  divided  by  the  number  of 
ohms  of  resistance  in  the  entire  circuit,  holds 
good  for  electrolytic  construction. 

,\  Resistance  of  Electrolytic  Cell. — In  view 
of  the  fact  that  it  is  the  amperage  of  the  cur 
rent  and  not  its  potential  which  determines 
I  the  rate  of  formation  of  hydrates,  it  is  obvious 
that  the  resistance  of  the  cell  should  be  kept 
as  nearly  as  possible  at  a  certain  minimum  for 
economical  reasons.  The  minimum  poten 
tial  is  determined  bv  the  polarization  of  the 
cell,  as  stated  more  fully  in  a  following  para 
graph.  The  resistance  of  the  cell  is  due  to 
several  factors,  among  which  are:  the  area 
of  electrodes:  the  distance  between  elec 
trodes;  the  amount  of  dissolved  salts  in  the 
river  water  (electrolyte):  and  the  formation 
of  non-conducting  coatings  on  the  electrodes. 
From  ( )hm's  law  it  follows  that  the  re 
sistance  of  an  electrolytic  cell  increases  di 
rectly  with  the  water  space  between  the  elec 
trodes,  and  inversely  with  the  cross-section 
of  the  electrolyte  (or  area  of  the  electrodes). 

./.  Resistance  to  the  Passage  of  an  Electric 
Current  of  Ohio  River  U'atcr. — This  subject 
has  been  referred  to  in  Chapter  XIII,  where 
it  was  seen  that  during  the  period  of  flood  in 
February  and  March,  1897,  the  resistance  of 
the  river  water  increased  nearly  threefold, 
due  to  the  decrease  in  amount  of  dissolved 
chemical  compounds.  That,  practically  speak 
ing,  the  suspended  matters  in  the  water,  m- 
cluding  those  partially  dissolved  constituents, 
exerted  no  influence  on  the  conductivity  was 
also  presented  at  that  time. 

Estimating  the  conductivity  or  resistance 
(which  is  the  reciprocal  of  the  conductivity) 
of  the  river  water  from  the  observations  on 
different  combinations  of  various  solutions  of 
the  salts  normally  present  in  it,  the  resistance 
in  ohms  per  centimeter  cube  should  be  theo 
retically  6100,  930,  and  2080  ohms  for  maxi 
mum,  minimum,  and  average,  respectively, 
corresponding  to  72,  2<K>,  and  122  parts  per 
million  of  dissolved  chemical  compounds,  not 
including  carbonic  acid-  gas.  As  will  be 
shown  in  connection  with  the  study  of  pas 
sivity  of  iron  electrodes,  it  is  not  possible  to 
draw  specific  mathematical  conclusions  in  re- 


SUMMARY  AND   DISCUSSION    OF  DATA    OF  1891 


39' 


gard  to  the  behavior  of  combinations  of  ions, 
based  on  the  results  of  observations  in  indi 
vidual  ions.  It  will  be  also  shown  in  this 
connection  that  dissolved  carbonic  acid  gas 
is  only  very  slightly  ionized,  and  from  a  prac 
tical  point  of  view  need  not  be  considered  as 
a  conductor  at  all. 

It  is  therefore  necessary  to  rely  upon  ob 
servations  on  the  river  water  itself,  though  as 
will  be  seen,  the  theoretical  and  observed  re 
sistances  follow  closely  the  same  curve. 

On  Feb.  22,  1897,  the  observed  resistance 
of  the  electrolyte  in  the  Brownell  cell  was 
7600  ohms  per  centimeter  cube,  and  on 
Feb.  27  this  figure  became  16.750.  The 
amounts  of  dissolved  chemical  compounds 
on  these  days  were  146  and  67  parts  per  mil 
lion,  respectively.  On  Feb.  17.  with  120 
parts  per  million  of  dissolved  compounds,  the 
resistance  wras  observed  to  be  9200  ohms. 

In  connection  with  the  devices  of  the 
Water  Company  the  average  resistance  was 
observed  to  be  about  7000  ohms  per  centi 
meter  cube,  when  the  river  water  contained 
about  130  parts  of  dissolved  solids. 

From  these  results  combined  with  numer 
ous  special  observations,  including  those  in 
Chapter  XIII,  it  is  estimated  that  the  maxi 
mum,  minimum,  and  average  resistance  of 
the  Ohio  River  water  as  an  electrolyte  would 
be  17000.  2000,  and  7000  ohms  per  centi 
meter  cube,  corresponding  to  67, 324,  and  130 
parts  per  million  of  dissolved  chemical  com 
pounds,  exclusive  of  carbonic  acid,  which,  as 
was  shown,  is  only  very  slightly  ionized.  In 
times  of  great  freshets  the  dilution  of  the 
compounds  in  the  river  water  might  be  so 
great  that  it  would  be  advisable  to  add  com- 
mont  salt  to  the  water  to  increase  its  con 
ductivity  to  the  normal.  Investigations 
during  the  heavy  freshet  of  February  and 
March,  1897,  showed  that  this  could  be  ac 
complished  by  the  addition  of  common  salt 
in  amounts  not  exceeding  5  grains  per  gal 
lon.  Such  additions  would  not  cause  the 
total  amount  of  salt  to  be  greater  than  was 
normally  present  in  the  river  water  during 
the  low  stages  of  the  river  in  the  fall  of  1895. 
5.  Polarization  of  Electrodes. — When  a  cur 
rent  of  electricity  flows  through  an  electro 
lytic  cell,  and  causes  changes  in  the  electrolyte, 
or  on  the  electrode,  the  electromotive  force 


of  the  current  is  thereby  reduced.  This 
action  is  known  as  polarization.  In  explana 
tion  of  this  point,  which  determines  the  mini 
mum  potential  of  current  that  can  be  safely 
employed,  it  is  to  be  stated  that  all  ions  pos 
sess  a  certain  force  or  intensity  of  fixation 
wherewith  they  attempt  to  retain  their  elec 
tric  charges  when  they  reach  the  electrodes. 
Accordingly,  a  certain  potential,  slightly 
above  that  corresponding  to  the  intensity  of 
fixation,  is  necessary  in  order  to  overcome 
this  force,  and  free  the  ions  at  the  electrodes 
of  their  electric  charges.  The  existence  of  this 
intensity  of  fixation,  with  an  opportunity 
to  measure  it,  is  shown  by  the  reverse  cur 
rent  which  takes  place  for  a  short  time  when 
the  primary  current  is  shut  off.  With  active 
electrodes,  polarization  becomes  less  marked. 
The  potential  of  polarization  varies  in  the  line 
of  work  in  question.  So  far  as  we  know, 
there  would  be  no  case  where  the  polarization 
would  require  over  2.35  volts  to  overcome  it. 
Ordinarily  it  would  be  much  less  than  this. 
Records  show  that  in  the  investigation  of 
electrolysis  of  iron  pipes  lying  in  the  ground 
near  electric  lines  of  street-cars  (a  subject" 
similar  in  a  measure  to  the  present  one),  de 
composition  of  the  iron  has  taken  place  at  a 
potential  of  only  o.ooi  volt.  In  all  cases  a 
difference  in  potential  of  2.5  volts,  or  less  be 
tween  adjoining  electrodes,  would  suffice  to 
overcome  the  intensity  of  fixation  of  all  ions, 
while  much  less  than  this  would  probably  be 
adequate  for  a  majority  of  the  ions.  Practi 
cal  investigations  along  this  line  are  recorded 
in  section  Xo.  4  of  this  chapter,  where  it  will 
be  seen  that  potential  differences  as  low  as 
r.o  volt  can  be  safely  employed  with  iron 
electrodes. 

6.  Passivity  of  Electrodes.  —  As  already 
stated,  all  negative  electrodes,  so  far  as  is 
known,  are  passive  to  the  ions,  and  certain 
positive  electrodes  such  as  iron  and  alumi 
num,  are  active.  From  Ampere's  law  it  fol 
lows  that  the  same  quantity  of  electric  cur 
rent  always  causes  in  electrolysis  the  same 
equivalent  amount  of  acid  ions  (anions)  to  go 
to  the  positive  electrodes,  and  have  their  elec 
tric  charges  neutralized.  They  then  pass 
into  the  atomic  state.  With  passive  elec 
trodes,  they  attack  water,  and  equal  currents 
produce  equal  amounts  of  oxygen  gas.  Pro- 


39a 


WATER   PURIFICATION  AT  LOUISVILLE. 


vided  that  active  electrodes  were  completely 
active  (not  at  all  passive  or  insoluble  under 
the  action  of  these  liberated  acid  atoms),  the 
amount  of  metal  decomposed  from  the  posi 
tive  electrode  would  also  be  proportional  to 
the  amperage  of  the  current,  and  to  the 
amount  of  liberated  acid  ions,  in  accordance 
with  Ampere's  law. 

In  the  case  of  iron  and  aluminum  elec 
trodes,  however,  experience  .shows  that  the 
metal  of  the  positive  electrodes  is  not  dis 
solved  in  quantities  proportional  and  equiva 
lent  to  the  total  quantity  of  acid  ions  liberated 
at  the  positive  electrode.  From  a  practical 
point  of  view  this  fact  is  a  matter  of  vital  im 
portance,  because  it  relates  to  the  amount  of 
hydrate  formed,  and  consequently  to  the  com 
mercial  merits  of  the  process.  Stating  this 
in  another  way,  we  may  say  that  only  a  por 
tion  of  the  current  forms  the  hydrate  of  the 
metal  used  as  the  positive  electrode;  and 
therefore  such  metals  as  iron  and  aluminum 
are  only  partially  active,  as  a  portion  of  the 
current  causes  the  formation  of  oxygen,  just 
as  in  the  case  of  completely  passive  electrodes, 
•such  as  carbon  or  platinum. 

It  follows  from  the  above  statements  of 
facts  that,  under  practical  conditions,  iron 
and  aluminum  electrodes  are  only  partially 
active,  and  when  employed  in  this  process 
utilize  efficiently  only  a  portion  of  the  cur 
rent.  Hence,  in  the  following  sections,  in 
which  this  process  is  described  in  detail,  use 
must  be  made  of  degree  of  activity  or  degree 
of  passivity  of  electrode.  In  view  of  the  fact 
that  the  latter  expression  is  in  use  by  chem 
ists,  we  shall  adopt  it  in  future  cases  where 
reference  is  made  to  this  phase  of  the 
process. 

The  degree  of  passivity  of  iron  and  alu 
minum  electrodes  is  due  to  the  two  following 
factors: 

1.  The  initial  passivity  of  the  metal  to  the 
various    acid    ions    naturally    present    in    the 
river  water.     Thus  it  is  well  known  that  hy 
drochloric  acid   has  a  higher  solvent  action 
on  these  metals  than  carbonic  acid. 

2.  The  acquired  passivity  of  the  metal  to 
the  various  acid  ions,  due  to  the  formation 
of  thin  films  of  metallic  oxide,  caused  by  the 
oxygen  formed  by  the  weaker  ions,  upon  the 
metal. 


In  practice  the  varying  composition  of  the 
river  water  caused  a  wide  range  in  the  rela 
tive  amounts  of  the  different  acid  ions,  and 
the  consequent  total  dissolving  action  upon 
the  electrodes.  Experience  shows  that  an 
other  important  factor,  especially  in  the  case 
of  aluminum,  is  the  fact  that  the  film  of  metal 
lic  oxide  on  the  positive  pole  causes  a  ma 
terial  increase  in  the  resistance  which  the 
electric  current  meets  in  its  passage  through 
the  cell.  In  the  case  of  iron  electrodes,  how 
ever,  this  is  relatively  slight,  owing  to  the  fact 
that  the  film  cracks  and  falls  off  in  scales  at 
frequent  but  irregular  intervals. 

7.  Secondary  Reactions.  —  Normally  there 
are  formed  with  active  electrodes  a  hydrate  of 
the  metal,  hydrogen,  and,  varying  with  the  de 
gree  of  passivity,  a  certain  amount  of  oxygen. 
These  reactions  have  been  explained  in  the 
foregoing  account  of  electrolysis,  and  may  be 
called  primary  reactions,  or  perhaps  the  pri 
mary  group  of  reactions.  Other  reactions  (in 
dependent  of  coagulation),  called  secondary 
reactions,  will  now  be  referred  to. 

When  iron  electrodes  are  employed  the 
iron  is  dissolved  from  the  plates  in  the  form 
of  ferrous  or  unoxidized  salts,  which  would 
be  converted  into  the  partially  soluble  ferrous 
hydrate  by  the  alkaline  hydrates  coming  from 
the  negative  electrode.  Accordingly,  oxy 
gen  is  necessary,  in  order  to  convert  the  fer 
rous  into  the  ferric  forms.  As  practically  all  of 
the  electrolytically  formed  oxygen  attacks  the 
positive  iron  electrodes,  it  is  necessary  that 
the  atmospheric  oxygen,  naturally  dissolved 
in  the  water,  serves  to  effect  this  oxidation. 
This  oxidation  is  necessary  in  order  to  con 
vert  the  iron  into  a  completely  insoluble 
form,  so  that  it  can  coagulate  the  suspended 
matter  in  the  water  without  any  dissolved 
iron  passing  through  the  filter  into  the  puri 
fied  water. 

The  secondary  reactions  in  the  case  of  alu 
minum  electrodes  are  less  clearly  understood, 
but  are  referred  to  beyond. 

Concerning  hydrogen  at  the  negative  elec 
trode,  small  portions  of  it  in  the  nascent  con 
dition  combine  with  atmospheric  oxygen 
dissolved  in  the  water,  and  reduce  iron  com 
pounds  and  nitrates;  while  the  bulk  of  it,  after 
saturating  the  pores  of  the  metal,  escapes  as 
a  gas  in  a  molecular  condition. 


SUMMARY  AND    DJSCUSS1ON   OF   DATA    Of-    18!  >f. 


393 


SECTION  No.  4. 

DETAILED  ACCOUNT  OF  THE  ELECTROLYTIC 

FORMATION  OF  IRON  HYDRATE  IN  THE 

OHIO  RIVER  WATER. 

A  full  record  and  discussion  of  this  process 
is  presented  under  several  leading  topics  as 
follows: 

Degree  of  Passivity  of  Iron  Electrodes  due  to 

the  Different  Acid  Ions  of  flic  Ohio 

Rh'cr  Water. 

The  dissolved  acids  which  are  present  in 
appreciable  amounts  in  the  Ohio  River  water 
are  hydrochloric,  sulphuric,  nitric,  silicic,  and 
carbonic. 

As  is  well  known  to  chemists,  these  acids 
differ  in  their  ability  to  dissolve  iron.  This 
capacity  of  being  dissolved  by  acids  under  the 
conditions  of  electrolysis  measures  the  pas- 
sivitv  of  iron  in  electrolvtes  containing  the 


acid  in  question.  Several  experiments  were 
made  in  which  solutions  containing  the  re 
spective  acids  alone  and  in  various  combina 
tions  (in  the  form  of  salts  of  the  alkalies)  were 
placed  in  sets  of  cells  containing  electrodes 
of  bright  wrought  iron  and  of  rusty  iron  from 
the  same  sheet.  The  cells  were  arranged  in 
series,  and  an  electric  current  of  from  2  to  47 
amperes  per  square  foot  was  passed  through 
them  for  periods  of  from  2  to  30  minutes. 

Aliquot  portions  of  the  contents  of  each 
cell,  after  rinsing-  the  electrodes,  were  col 
lected  for  determinations  of  the  amounts  of 
iron.  The  average  results  of  these  determina 
tions,  together  with  the  average  specific  re 
sistances  of  the  several  electrolytes,  are  pre 
sented  in  the  following  table. 

Percentages  which  the  metal  decomposed 
was  of  the  theoretical  rate  (1.05  grams  per 
ampere  hour)  are  also  given. 

The  potential  difference  between  the  plates 
varied  in  these  experiments  from  12  to  220 
volts. 


SUMMARY   OF    RESULTS    SHOWING    AVERAGE    RATES    OF    ELECTROLYTIC    DECOMPOSITION    OF 
NEW   AND    OLD    IRON    IN    ELECTROLYTES    OF    VARIOUS    ACID    IONS. 


Avc 

ras;e  Kate  of 

Decomposi 

A  Venice 

Acid  Ions. 

Parts  per 
Million.* 

Grams  pc 
Ho 

r  Ampere- 
ur.t 

Per  Cen 
Theoreti 

t.  of  the 
Ciil  Rate. 

of 
Klectrnlytc. 
Ohms  per 

New  Iron. 

Old  Iron. 

New  Iron. 

Old  Iron. 

Cube. 

o  85 

88 

8l 

6880 

69 

60 

0  86 

82 

76 

(>-> 

D 

75 

6960 

L 

1  .00 

0.63 

95 

60 

3  3<>° 

IO  , 

e    f 

I  .  12 

0.90 

107 

86 

4170 

IO  , 

60  f 

0.97 

0.64 

93 

61 

I  690 

10  | 

0.90 

0-73 

86 

70 

iol 

5 

5 

1.04 

0.44 

99 

42 

I  240 

60  1 

5 

. 

\\ 

1  .03 

0.48 

98 

46 

1310 

60  | 

1  Carbonic  acid  (dissolved  gas)  

50  J 

*  These  quantities  are  equivalent  to  the  estimated  average  amounts  of  the  several  acids  contained  in  the  Ohio 
River  water. 

f  To  change  grams  per  ampere-hour  into  grains  per  ampere-hour  multiply  by  15.4. 


394 


WATER   PURIFICATION  AT  LOUISVILLE. 


The  above  data  indicate  quite  clearly  one 
point  which  is,  that  the  result  of  combinations 
of  two  or  more  ions  under  these  conditions 
is  not  the  mathematical  result  of  their  sum 
except  by  chance.  If  the  observations  of  the 
resistances  of  the  combined  electrolytes 
(chlorine  with  the  other  ions)  be  compared 
it  will  be  seen  that  there  is  a  marked  differ 
ence  from  the  theoretical  resistance  of  the 
combinations. 

The  only  apparent  explanation  to  account 
for  this  is  that  when  two  or  more  ions  are 
combined  in  these  amounts  in  the  same  elec 
trolyte  their  degrees  of  ionization  are  differ 
ent  than,  in  the  case  when  any  one  of  them  is 
presented  alone. 

The  relation  between  the  calculated  and 
observed  results  becomes  then  a  somewhat 
variable  one,  dependent  upon  the  relative  de 
grees  of  ionization  of  the  several  acids. 

The  conclusions  which  may  be  drawn  from 
these  experiments  are  that  the  relative 
amounts  of  the  different  ions  present  in  the 
river  water  would  affect  the  rate  of  decom 
position,  but  the  influence  of  the  several  fac 
tors  under  practical  conditions  is  so  variable 
that  the  present  data  are  insufficient  to  deter 
mine  the  exact  laws  for  the  estimation  of 
these  amounts. 

Cause  of  Passivity — Initial  and  Acquired. 

In  the  last  section  a  table  of  results  was 
presented  of  some  experiments  with  new 
bright  wrought-iron  and  old  (rusty)  iron  elec 
trodes.  Both  sets  were  cut  from  the  same 
plate,  and  one  set  cleaned  to  bright  metal 
while  the  other  remained  rusty.  It  will  be 
seen  that  the  results  of  observation  on  the 
behavior  of  the  new  iron  gave  rates  of  de 
composition  varying  from  79  per  cent,  of  the 
theoretical  with  silicic  acid  to  1 1 1  per  cent, 
with  dissolved  chlorides,  averaging  90.5  per 
cent.  That  new  bright  iron  behaves  differ 
ently  toward  the  several  ions  is  clearly  shown, 
and  while  it  is  difficult  to  account  for  the  re 
sults  over  100  per  cent.,  it  seems  clear  that  in 
the  case  of  all  but  hydrochloric  acid  a  certain 
percentage  of  the  electric  current  is  not  di 
rectly  utilized  in  dissolving  the  metal.  The 
explanation  of  this  lies  in  the  relative  affinities 
of  these  ions  for  the  metal  and  for  water. 
When  the  electric  current  is  transferred  by 


means  of  the  ions  and  the  ions  are  discharged 
or  neutralized  at  the  positive  pole,  they  attack 
the  water  of  the  electrolyte  and  the  metal  in 
the  proportion  of  their  affinities  for  the  liquid 
and  the  metal.  The  acid  ions  which  attack  the 
water  can  be  said  to  represent  the  passivity 
of  the  iron,  because  they  would  attack  the 
iron  were  it  not  passive.  The  results  on  new 
iron  may  be  taken  to  indicate  the  relative 
passivities  which  bright  iron  has  to  the  sev 
eral  acid  ions.  The  data  are  not  sufficient, 
however,  to  warrant  the  use  of  these  figures 
except  in  a  comparative  manner. 

Those  ions  to  which  the  metal  is  passive 
attack  and  decompose  water,  setting  free  oxy 
gen  gas  in  a  nascent  condition.  Between 
this  gas  and  the  metal  there  is  at  all  times 
great  affinity,  and  therefore  a  considerable 
amount  of  the  oxygen  attacks  the  metal  and 
forms  the  oxide.  As  this  continues  the  plate 
becomes  covered  with  a  coating  of  oxide 
scale  which  grows  thicker  and  thicker  until 
it  begins  to  crack  off.  Practically  speaking, 
the  rate  at  which  the  scale  is  removed  from 
the  plate  by  cracking  and  peeling  becomes 
eventually  as  great  as  the  rate  of  its  forma 
tion,  and  equilibrium  is  established  with 
reference  to  the  respective  attacking  of  the 
metal  and  of  water. 

The  presence  of  this  oxide  scale  changes 
the  relation  of  the  acid  ions  to  the  metal,  as 
they  must  either  attack  and  dissolve  the  oxide 
or  pass  through  the  scale  to  attack  the  pure 
bright  metal  beneath.  As  either  of  these 
processes  requires  more  energy  than  the  sim 
ple  solution  of  the  metal,  an  increased  per 
centage  of  the  ions  does  not  attack  the  metal, 
but  decomposes  water,  and  by  this  action  the 
iron  has  an  acquired  passtivity. 

During  the  process  of  formation  of  the 
scale  and  before  equilibrium  has  been  estab 
lished  between  the  formation  of  the  oxide  and 
its  scaling  off,  the  acquired  degree  of  passiv 
ity  increases  rapidly  as  the  scale  forms. 

As  the  formation  of  the  oxide  is  dependent 
on  the  passivity  of  the  metal  and  this  in  turn 
increases  with  the  oxide  present  on  the  face 
of  the  plate,  the  process  is  a  reciprocal  one, 
one  action  increasing  the  other.  For  this 
reason  the  length  of  time  elapsing  between 
the  beginning  and  end  of  the  action  (estab 
lishment  of  equilibrium)  is  comparatively 


SUMMARY  AND   DISCUSSION   OF  DATA    OF   1897. 


395 


short  and  is  dependent  upon  the  density  of 
the  current  used.  Furthermore,  it  is  proba 
ble  that  the  passivity  of  the  metal  may  be 
come  greater,  before  the  scale  begins  to  come 
off,  than  it  is  after  equilibrium  has  been  estab 
lished. 

The  results  with  old  iron,  presented  in  the 
last  section,  may  be  taken  as  fairly  representa 
tive  of  the  total  passivity  of  iron  as  it  would 
be  used  in  practice. 

As  will  be  presented  beyond,  there  are  no 
indications  to  warrant  the  belief  that  the  po 
tential  difference  between  the  plates  has  any 
effect  upon  the  passivity  of  the  metal. 

Within  the  limits  employed  in  these  inves 
tigations  the  difference  in  initial  passivity 
due  to  the  composition  of  the  metal  was  not 
apparent,  cast  iron,  wrought  iron  of  different 
grades,  and  mild  steel  all  giving  apparently 
parallel  results,  or  very  nearly  so. 


Form  in  which  Iron  leaves  the  Plates. 

The  iron  leaves  the  positive  electrodes 
only,  and  in  order  to  make  the  full  set  of 
plates  serviceable  it  is  necessary  to  reverse 
the  electric  current  from  time  to  time. 

At  the  positive  electrodes  the  iron  leaves 
the  plates  in  two  ways,  namely: 

1.  Those  acid  ions,  which  are  neutralized 
electrically  at  the  pole  by  dissolving  some  of 
the  metal,  form  iron  salts  of  the  various  acids, 
such  as  iron  chloride,  iron  sulphate,  and  iron 
carbonate.     These  compounds,   furthermore, 
are  in  the  ferrous  (unoxidized)  condition,  as 
explained  in  the  next  section. 

2.  Those  acid  ions  which,  by  virtue  of  the 
degree  of  passivity  of  the  iron  anode,  find  it 
easier  to  react  with  water  upon  neutralization 
than   to  dissolve  the  equivalent  amounts  of 
iron,  form  oxygen.     This  oxygen  unites  with 
the  iron  to  form  iron  oxide,  which  appears  as 
films. 

In  the  first  case  the  solution  of  iron  is  regu 
lar  and  proportional  to  the  amperage  of  the 
current  when  the  degree  of  passivity  is  con 
stant.  With  those  ions  to  which  the  iron 
electrode  is  passive,  the  formation  of  films 
of  iron  oxide  is  regular,  but  the  films  crack 
and  peel  off  from  the  electrode  in  an  irregular 
manner. 


Influence  on  the  Process  of  O.v\gcn. 

With  the  Ohio  River  water  the  oxygen  in 
an  electrolytic  cell  comes  from  two  sources, 
the  atmospheric  oxygen  naturally  dissolved 
in  the  water,  and  the  oxygen  which  is  formed 
eleectrolytically  at  the  anode.  We  shall  con 
sider  them  separately. 

Atmospheric  O.rygcn. —  The  atmospheric 
oxygen  performs  a  very  important  part  in  this 
process,  by  virtue  of  the  fact  that  it  unites 
witli  the  ferrous  compounds  as  they  are  dis 
solved  from  the  electrode,  and  changes  them 
to  ferric  or  oxidized  salts  of  iron.  Appar 
ently  this  action  takes  place  partly  before  the 
iron  salts  are  acted  upon  by  the  alkaline  hy 
drates  coming  from  the  negative  pole,  and 
partly  after  this  reaction. 

The  result  is  that  after  the  completion  of 
the  secondary  group  of  reactions,  the  dis 
solved  iron  is  converted  into  the  form  of  in 
soluble  ferric  hydrate,  which  is  an  excellent 
coagulant.  The  importance  of  this  oxida 
tion  from  a  practical  point  of  view  is  great, 
because  without  it  ferrous  hydrate  alone 
would  be  formed;  and,  owing  to  its  partial 
solubility,  there  would  be  difficulties  arising 
from  its  passage  through  the  filter. 

A  small  amount  of  atmospheric  oxygen 
also  unites  with  hydrogen,  which  is  given  off 
as  a  gas  at  the  negative  electrodes.  As  this 
combination  cannot  take  place  except  when 
the  hydrogen  is  in  the  nascent  state,  the  ac 
tion  is  confined  to  the  oxygen  in  the  immedi 
ate  vicinity  of  the  cathode. 

Electrolytic  O.rvgcn. — So  far  as  could  be 
learned,  practically  all  of  the  oxygen  which  is 
formed  at  the  anode  by  the  decomposition  of 
water  attacks  the  metal  electrodes  and  forms 
films  of  iron  oxide.  As  stated  above,  these 
films  crack  off  and  leave  the  cell  in  an  ir 
regular  manner. 

Of  course  the  scales  or  films  of  iron  oxide 
are  of  no  assistance  in  the  purification  of 
water. 

Comparing  the  influence  of  the  oxygen 
from  the  two  sources  we  see  that  the  atmos 
pheric  oxygen  performs  a  very  important 
part,  and  without  it  the  process  could  not  be 
put  in  practice  with  satisfactory  results.  The 
influence  of  the  electrolytic  oxygen  and  the 
factors  which  produce  it,  on  the  other  hand. 


396 


WAT  lilt   PURIF1CA1ION   AT  LOUISVILLE. 


is  a  very  serious  drawback  to  the  process,  be 
cause  it  means  a  large  waste  of  electric  power 
and  of  metallic  iron.  The  amount  of  power 
and  of  metal  wasted  is  shown  bevond. 


Viewed  in  the  present  connection,  as  a  fac 
tor  in  a  series  of  secondary  reactions  which 
occur  in  this  process  after  the  iron  is  dis 
solved  from  the  anode,  carbonic  acid  did  not 
give  indications  of  retarding  the  oxidation  of 
the  resulting  ferrous  salts,  as  was  the  cas'e 
when  commercial  protosulphate  of  iron  (cop 
peras)  was  applied  to  the  water.  So  far  as 
could  be  learned  the  practical  effect  of  car 
bonic  acid  upon  any  secondary  reaction  was 
ml. 

With  regard  to  the  relation  of  free  carbonic 
acid  to  the  passivity  of  iron  electrodes  and  the 
degree  of  its  ionization,  the  evidence  has  al 
ready  been  presented.  Briefly,  it  showed 
that  the  degree  of  ionization  of  free  carbonic 
acid  in  the  water  is  very  low,  and  in  this  con 
nection  its  practical  significance  is  very 
slight. 


Under  all  conditions  hydrogen  gas  is  pro 
duced  at  the  negative  electrode  in  amounts 
proportional  to  the  formation  of  alkaline  hy 
drates.  Owing  to  the  fact  that  iron  pos 
sesses  the  capacity  to  occlude  large  quanti 
ties  of  hydrogen  gas  within  its  pores,  a 
portion  of  the  hydrogen  is  disposed  of  in  this 
manner,  and  there  are  reasons  for  believing 
that  the  negative  electrode  after  a  time  is 
practically  composed  of  hydrogen,  from  an 
electrical  point  of  view.  A  small  portion  of 
the  hydrogen  when  in  a  nascent  condition 
unites  with  atmospheric  oxygen  to  form 
water.  The  bulk  of  it,  however,  after  the 
saturation  of  the  pores  of  the  iron  cathode 
and  of  the  water,  escapes  as  a  gas. 

The  only  practical  influence  of  hydrogen, 
other  than  the  slight  consumption  of  the  at 
mospheric  oxygen,  is  in  connection  with  sub 
sequent  sedimentation  and  filtration,  as  men 
tioned  beyond,  together  with  the  relation  of 
other  factors  of  the  process  upon  the  follow 
ing  'steps  in  the  purification  of  water. 


It  has  been  stated  that  when  the  iron  is  first 
dissolved  from  the  positive  electrode  the 
compounds  are  in  a  form  of  soluble  ferrous 
salts.  Experience  shows  that  some  of  these 
iron  salts,  before  they  are  converted  into  in 
soluble  ferric  hydrate,  become  conductors  of 
the  electric  current  just  like  lime  and  other 
salts  dissolved  in  the  water.  The  result  of 
this  is  that  a  portion  of  the  iron  is  conducted 
to  the  negative  electrode;  and,  in  a.  manner 
similar  to  that  in  electroplating,  is  deposited 
there  in  what  appears  to  be  a  metallic  form. 

From  a  practical  point  of  view  the  influ 
ence  of  this  state  of  affairs  is  to  cause  a  waste 
of  electric  current,  as  no  good  is  accom 
plished  by  transferring  the  metal  from  one 
pole  to  the  other.  So  far  as  could  be  learned 
this  metal  is  not  wasted,  but  is  available  for 
electrolytic  decomposition  when  the  direction 
of  the  electric  current  is  reversed. 

Form  in  which  the  Iron  leaves  the  Cell. 

A  portion  of  the  iron  which  leaves  the  cell 
is  in  a  form  available  for  coagulation,  while  a 
portion  is  not  available.  We  shall  consider 
the  two  separately  in  this  connection. 

Available  Iron. — Analyses  of  the  treated 
water  as  it  leaves  the  cells  show  that  the 
greater  proportion  of  the  available  iron  com 
pounds  is  in  the  form  of  ferric  hydrate.  Some 
of  the  iron  which  may  be  actually  available 
for  coagulation  a  little  farther  along  in  the 
flow  of  the  water  is  at  times  in  the  form  of 
ferrous  compounds  as  the  water  leaves  the 
cell.  At  no  time  in  regular  practice  was  the 
amount  of  iron  in  the  form  of  ferrous  com 
pounds  found  to  exceed  3.8  parts  per  million. 
Lender  these  conditions  it  is  probable  that  all 
the  ferrous  iron  was  in  the  form  of  hydrate. 
When  the  rate  of  electrolytic  treatment  is  so 
great  that  the  atmospheric  oxygen  is  all  util 
ized,  then  additional  treatment  causes  the 
iron  to  leave  the  cell  in  the  form  of  ferrous 
hydrate.  Under  these  conditions  there  would 
be  about  seven  parts  per  million  of  iron  which 
would  be  soluble. 

Non-Available  Iron. — As  a  consequence  of 
the  passivity  of  iron  and  the  formation  of 


SUMMARY   AND   DISCUSSION   OF  DATA    OF  1X'J7. 


397 


films  or  scales  of  oxide  of  the  metal,  a  portion 
of  the  iron  leaves  the  cell  at  irregular  inter 
vals  in  the  form  of  flakes  or  scales. 

The  evidence  showing  the  relative  amounts 
of  iron  in  these  t\vo  forms  is  presented  just 
below. 

Natural  Limitations  of  the  Electrolytic   Treat 
ment  n'ith  Iron  Electrodes. 

From  the  foregoing  account  of  this  process 
it  is  clear  that  this  treatment  cannot  be  safely 
applied  beyond  the  point  where  atmospheric 
oxygen  in  the  water  is  entirely  utilized  to 
convert  the  iron  compounds  into  the  form  of 
insoluble  ferric  hydrate.  The  limit  of  safe  ap 
plication  of  this  process  depends  therefore  on 
two  factors,  namely,  the  rate  of  formation  of 
iron  compounds  and  the  amount  of  oxygen 
in  the  water;  both  of  these  vary,  and  their 
mutual  relation  is  referred  to  beyond,  after 
the  presentation  of  further  evidence. 

Rate  of  Decomposition  of  Iron  at  the  Positive 
Electrode. 

Owing  to  faulty  insulation  of  the  large 
electrodes  the  data  prior  to  May  29,  when 
hard  rubber  fittings  were  put  in  service,  are 
disregarded.  In  the  following  tables  the 
weights  of  iron  decomposed  electrolytically 
from  the  positive  electrodes  of  each  of  the 
two  sets  are  recorded  for  the  several  periods 
between  weighings,  together  with  the  corre 
sponding  electric  current  (expressed  in  am 
pere-hours)  for  each  period. 

During  the  first  week  of  June  the  sets  of 
electrodes  were  weighed  nearly  every  day, 
after  washing  with  a  stream  of  water  from  a 
hose.  It  was  found,  however,  that  these 
weighings  were  of  no  account,  owing  to  the 
metal  deposited  on  the  negative  electrodes 
and  to  remaining  accumulations  of  mud  and 
silt.  In  a  number  of  cases  such  weighings 
showed  an  increase  in  the  weight  of  the  elec 
trodes.  'Beginning  June  9,  the  electrodes 
were  dismantled  from  time  to  time  and  the 
positive  and  negative  plates  weighed  sepa 
rately,  after  cleaning  each  one  carefully  with 
a  broom  and  a  stream  of  water.  After  June  16 
the  direction  of  the  electric  current  was  re- 
reversed  from  time  to  time,  and  the  positive 
and  negative  plates  were  also  weighed  sepa 


rately  from  time  to  time.  The  periods  of 
service  between  weighings  were  considerably 
longer  than  formerly,  and  an  effort  was  made 
to  choose  such  times  for  weighing  when  the 
amount  of  metal  deposited  on  the  negative 
plates  formed  a  comparatively  small  per  cent, 
of  the  total  loss  of  metal.  Afrer  June  29  the 
plates  were  not  weighed  until  Sept.  25.  when 
the  entire  electric  plant  was  finally  dismantled. 
From  the  close  of  the  regular  tests  until 
Sept.  25  the  electrodes  were  used  for  several 
special  tests  and  exhibitions,  the  last  of  which 
was  on  Sept.  23.  When  not  in  service  the 
water  was  drawn  out  of  the  cells  in  which  the 
electrodes  were  placed. 

In  studying  the  following  table  it  is  to  be 
recalled  that  the  rate  of  decomposition  of 
iron  at  the  positive  electrode  would  be  16.2 
grains  (1.05  grams)  per  ampere-hour,  pro 
vided  that  the  iron  plates  were  completely 
active,  or.  in  other  words,  soluble  in  the  acid 
ions  discharged  at  that  point.  For  conve 
nience  in  comparison  this  is  called  the  theo 
retical  rate  of  decomposition. 

SUMMARY    OF    RESULTS. 


I'er 

ocl. 

Electric 

p'ofitive 

Average  Rate  of 
Decomposition. 

Per  Tent. 

of 
Theo. 

Grains 

Grams 

retical 

1                   1 

Electrodes   No.    1  , 

May 

)une 

*l\ 

46  760 

50.0 

7-5 

0.49              46 

,u 

34  '00 

86.5 

17.8 

i  .  1  6            no 

2  1 

23  660 

78.75 

23.3 

1.52            144 

2g  (-       3'  520         72.75         16.2 

1.05                loo 

Sept 

*9  |     109500,     288.25*      18.4          1-19            »3 

Totals 

245540       576.25 

16.42 

1.07 

102 

June 

E 
n't"        '5  75° 

ectrodes 

30.5 

No.    3. 

13.6 

0.88 

84 

II   / 

18  |" 

46  750 

104.0 

15.6 

i  .02 

96 

2Q  f        23  600 

46.0 

13  6 

0.88 

84 

Sept 

2J?  j-          72  420 

200.25 

19.4 

1.36 

12O 

Totals         158  500 

380.75* 

16.82 

1.09 

104 

Total  for  both  Electrodes. 

404040       957-00 

16.57 

1.075 

102 

*  Plates  scraped  with  metal  scrapers. 


WATER  PURIFICATION  AT  LOUISVILLE. 


The  slight  excess  of  the  total  average  rate 
of  decomposition  over  the  theoretical  was 
probably  due  largely  to  the  fact  that  at  the 
close  of  the  test  the  plates  were  freer  from 
rust  than  at  the  beginning  of  these  tests,  as  at 
the  close  the  plates  were  cleaned  with  me'.al 
scrapers.  Similarly  the  irregularities  in  some 
of  the  periods  were  due  largely,  if  not  wholly. 
to  different  degrees  of  thoroughness  with 
which  th:?  plates  were  cleaned  with  a  broom 
and  a  stream  of  water. 


The  rate  at  which  the  iron,  removed  from 
the  positive  electrodes  in  a  soluble  form,  may 
become  a  conductor  of  the  electric  current 
and  may  be  deposited  in  the  metallic  state, 
is  indicated  by  the  following  summary: 

SUMMARY    OF    RESULTS. 


Owing  to  the  fact  that  it  was  found  advis 
able  to  reverse  the  direction  of  the  electric 
current  at  the  end  of  the  above  period,  no 
further  data  upon  this  point  were  obtained. 
It  is  possible  that  slight  amounts  of  silt  from 
the  river  water  were  mixed  with  the  deposited 
metal,  and  caused  the  above  results  to  be  a 
trifle  high.  This  was  not  a  serious  factor, 
however,  because  the  river  water  at  this  time 
was  very  clear,  comparatively  speaking. 

During  the  above  periods  the  current  den 
sity  was  varied  from  time  to  time.  On  elec 
trodes  No.  i,  from  May  29  to  June  7,  the 
current  ranged  from  100  to  400  amperes  and 
averaged  253  amperes,  corresponding  to  0.26, 
1.03,  and  0.65  amperes  per  square  foot  of  the 
active  surface  of  the  cathodes  (corresponding 
approximately  to  the  cross-section  of  the 
electrolyte).  With  electrodes  No.  3  for  the 
above  period  the  maximum,  minimum,  and 


average  currents  were  234,  171,  and  196  am 
peres,  respectively,  corresponding  to  0.60, 
0.44,  and  0.50  amperes  per  square  foot  of 
cathode  surface.  From  May  29  to  June  2, 
inclusive,  it  required  about  O.8  minute  for  the 
water  to  pass  through  the  portion  of  cell  No. 
i  occupied  by  the  electrodes.  From  June  2 
to  9  the  rate  of  (low  in  both  cells  Nos.  i  and  3 
was  such  that  the  water  remained  in  the  por 
tion  of  these  cells  occupied  by  the  electrodes 
for  about  i  minute.  With  the  same  rate  of  flow 
of  water  through  a  cell,  it  is  probable  that  the 
rate  of  deposition  of  metal  would  increase  di 
rectly  with  the  current  density  and  with  the 
specific  resistance  of  the  electrolyte.  For  the 
composition  of  the  river  water  at  this  time 
sec  Chapter  J. 


oi 

Average  Rate  of 

-3 

Gain  in                    Deposition. 

§ 

Period. 

Electric 
Current 

WeiKlH  of 
Negative 

Per  Ampere- 

PerCent. 

W 

Ampere- 

trodes. 

Ilour. 

of  Theo- 

f 

1  tours. 

Pounds. 



Decom 

Jj 

Grain*.    Grams. 

position. 

I 

May    29  | 
June     9  f 

46  760 

14.0 

2.1        0.14 

S.6 

3 

June     2  I 
June     7  )" 

15  730 

6.0 

2.7      o  .  I  S 

II  .  I 

\Ye  have  considered  the  rate  of  decompo 
sition  of  iron  at  the  positive  electrode,  some 
of  which  is  non-available  for  coagulation,  as 
it  is  in  the  form  of  scales  of  iron  oxide,  and 
the  deposition  of  some  of  the  soluble  iron, 
capable  of  forming  ferric  hydrate,  at  the  nega 
tive  electrode.  It  remains  to  show  the  rate 
of  formation  of  iron  hydrate  which  is  the  only 
form  capable  of  coagulating  the  river  water. 
From  time  to  time  during  the  regular  opera 
tion  the  amount  of  iron  leaving  the  cell  was 
determined  by  tests  with  ferricyanide  and 
ferrocyanide.  By  these  well-known  tests  it 
was  learned,  in  addition  to  the  total  amount. 
how  much  iron  was  in  the  two  states  of  oxi 
dation  (ferrous  and  ferric  iron).  But  these 
tests  do  not  show  the  difference  between  the 
hydrate  and  the  scales  of  oxide  which  are 
given  off  at  an  irregular  rate.  To  note  the 
rate  of  hydrate  formation  it  is  necessary  to 
compare  a  series  of  observations,  and  study 
the  low  and  uniform  rates,  which  are  affected 
but  little,  comparatively  speaking,  by  scales 
of  oxide. 

In  order  to  make  this  evidence  as  complete 
as  practicable,  numerous  special  tests  with 
electrodes  Nos.  i  and  3  were  begun  on  Jn'y 
23  and  continued  until  July  28.  The  results 
of  these  tests,  with  the  percentage  which  the 
total  iron  was  of  the  amount  indicated  by  the 
theoretically  normal  rate  of  formation,  are 
presented  in  the  set  of  tables  on  pages  400 


SUMMARY  AND   DISCUSSION  OF  DATA    OF  1897. 


399 


and  401.  In  these  tables  sufficient  notes  will 
he  found  to  make  plain  the  conditions  of 
operation. 

It  will  be  seen  that  the  results  of  these  tests, 
which  confirm  earlier  and  more  fragmentary 
data,  indicate  a  normal  amount  of  iron  in  the 
water  leaving  the  cells,  or  something  less  than 
50  per  cent,  of  the  quantity  corresponding  to 
the  theoretical  rate  of  decomposition.  In 
some  instances  the  amount  of  iron  exceeded 
100  per  cent,  of  the  theoretical  rate,  showing 
an  abnormal  removal  of  scale  of  oxide.  So 
far  as  could  be  learned  the  amount  of  iron 
corresponding  to  more  than  about  50  per 
cent,  of  the  theoretical  rate  was  ordinarily 
present  for  the  most  part  in  the  form  of  scales. 
At  times  it  will  be  seen  that  the  rate  was  con 
siderably  less  than  40  per  cent.  Among  the 
principal  factors  which  aided  in  producing  the 
low  results  are  the  reversal  of  the  electric  cur 
rent,  exposure  of  the  plates  to  air  when  not 
in  service,  and  coatings  of  mud  mixed  with 
the  scale  and  films.  These  factors  are  re 
ferred  to  beyond  the  tables. 

At  the  beginning  of  these  experiments 
electrodes  Xo.  3  were  dry,  not  having  been 
used  since  8.30  P.M.,  July  16.  Electrodes  No. 
i  had  been  in  use  on  July  22  and  had  only 
partially  dried  off  during  the  night.  Through 
out  this  series  a  uniform  rate  of  flow  of  water 
of  23.5  cubic  feet  per  minute  through  each 
cell  was  maintained  while  in  operation.  At 
the  start  a  current  of  210  amperes  was  used, 
which  gave  an  effective  current  of  0.020  am 
pere-hour  per  gallon  in  cell  Xo.  3,  and  0.040 
ampere-hour  per  gallon  in  cell  Xo.  i,  which 
contained  the  modified  electrodes  Xo.  i. 
The  potential  difference  between  the  plates  at 
the  start  (at  210  amperes)  was  6  volts  on  Xo. 
i  and  4  volts  on  Xo.  3.  When  the  current 
was  increased  on  July  23  to  400  amperes  the 
potential  differences  were  increased  to  1 1  and 
6  respectively.  The  current  density  at  210 
amperes  was  0.51  ampere  per  square  foot  of 
anode  in  electrodes  Xo.  3  and  i.oo  ampere 
per  square  foot  of  anode  in  modified  elec 
trodes  Xo.  i.  The  corresponding  figures  for 
400  amperes  were  0.97  and  1.91,  respectively. 

Influence  on  the  I'onnatioii  of  Hydrate  of  Po 
tential  Difference  bctiwcn  the  Plufes. 
Potential  difference  can  be  denned  as  the 


electric  pressure  necessary  to  cause  the  pas 
sage  of  the  desired  strength  of  electric  cur 
rent  through  the  electrolyte  from  plate  to 
plate  of  the  electrodes.  This  pressure 
is  necessary  to  cause  the  ions  to  carry 
their  respective  charges  to  the  poles,  and 
is  therefore  dependent  on  the  density  of 
the  current  and  length  of  the  electrolyte. 
There  is,  furthermore,  a  certain  potential 
difference  necessary  to  overcome  the  resist 
ance  which  the  ions  have  against  neutrali 
zation.  This  is  the  polarization  resistance. 
In  the  case  of  passive  electrodes  the  available 
data  indicated  that  as  a  maximum  this  resist 
ance  may  reach  as  high  as  2.35  volts;  and  in 
practice  it  was  assumed  early  in  these  tests 
that  3  volts  was  the  lowest  safe  minimum  dif 
ference  in  potential  to  secure  a  utilization  of 
all  ions  uniformly. 

So  far  as  could  be  learned  the  practical  in 
fluence  upon  the  formation  of  hydrate,  of  the 
potential  difference  above  this  limit,  is  ;///. 
During  the  use  of  the  large  electrodes  poten 
tial  differences  between  the  plates  of  from  3 
to  12  volts  were  employed.  In  laboratory  ex 
periments  the  potential  difference  was  carried 
at  times  as  high  as  220  volts,  although  the 
usual  range  was  from  20  to  50  volts. 

The  most  serious  factor  against  the  econ 
omy  of  this  process  of  formation  of  coagu 
lants  is  the  passivity  of  the  iron  to  the  various 
dissolving  ions  in  the  river  water.  As  has 
been  shown  in  previous  portions  of  this  dis 
cussion,  the  passivity  of  iron  is  represented  by 
the  percentage  which  the  actual  amount  de 
composed  and  converted  into  hydrate  is  of 
the  total  theoretical  rate  of  decomposition, 
and  ranged  during  the  observations  on  this 
point,  including  laboratory  tests,  from  about 
30  to  50. 

As  the  ions  which  do  not  dissolve  the  metal 
attack  water,  it  appeared,  as  the  report  on 
these  matters  neared  completion,  that  by  low 
ering  the  potential  difference  to  an  amount 
below  that  which  is  commonly  accepted  as 
necessary  to  maintain  a  steady  decomposition 
of  water,  with  passive  electrodes,  this  partial 
passivity  of  active  electrodes  might  be  over 
come  in  a  measure. 

For  this  purpose  two  electrodes  of  steel 
were  prepared  and  operated  from  1.20  P.M, 
Sept.  28,  to  9.00  A.M.,  Sept.  30.  The  area 


400 


WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE    SHOWING     THE    CONDITION    OF    OXIDATION    AND     AMOUNTS    OF     ELECTROLY TICALLY 

DECOMPOSED    IRON    LEAVING    THE    CELLS,    EXPRESSED    IN     PARTS     PER     MILLION 

AND     IN    PERCENTAGES    OF    THE   THEORETICAL    RATE. 


Cell  No.  i. 

Cell  No.  3. 

Dale. 

Hour. 

Parts  per  Mi  lion. 

J  jii  — 

Parts  per  M 

lion. 

S(S  g  . 

Remarks. 

1897. 

5^3- 

U  v  I  -. 

Ferrous 

Ferric      Total 

£•2  oS. 

Ferrous 

Ferric 

Total 

t  -  co: 

Iron. 

Iron. 

Iron. 

a. 

Iron. 

Iron. 

Iron. 

SH 

Conditions  at  start  described  in  text. 

JU  1  V   °  "\ 

nee    A    M 

0  .  5 

S.o        8.  5 

77    :  .  . 

uiy    43                -J-JJ    ....... 
"       23                 O.O5         " 

I  .  O 

9  -  o      10.  o 

"      23              0.2O       " 
•  '       03               ().  ^O        '  ' 

o.5 
o  •  3 

n.  o      11.5 

11    O         111 

104        o.o 

I  20 

IO.O 

IO.O 

7° 

"       23        ,        1.  06        " 

O.  I 

1  J  •  ^        A  J  •  J 
IO.O        IO.I 

91      0.4 

10.0      10.4 

73 

'  '     23      '      1  .47      '  ' 

o.  3 

S.o        8.3 

75      

"23            .57     " 

o.  3 

R  .  o         S.i 

75     

"      23              2.25    P.M. 

o.o        5.5        5.5 

50       o.o 

9.0        9  .  o 

63 

"       23                T.OO        " 

0.3      10.  o      10.3 

93        0.3 

10.0      10.3 

72 

"       23                   .20        " 

0.2    |       9.0           9.2 

83 

O.O 

9-5         9-5 

67 

"       23                I.5<)        " 

O.  I 

9.0      9.  1 

82     :        O.I 

9-5         <)•(> 

67 

"       23               2.05        " 

0.4 

9.0      9.4 

85 

0-3 

9.0        9.3 

6; 

"      23              2.20       " 

0.4 

7-5 

7-9 

71 

0.4 

7-5        7-9 

56 

"      23              2.35       " 

0-3 

7.0 

7-3 

66 

o-3 

7.0 

7-3 

51 

"      23              2.50 

0.3 

7-0 

7-3 

66        0.2 

7-5 

7-7 

54 

"      23              3.05       " 

0.2 

7.0 

7-2 

65 

0.3 

7-2        7-5 

53 

"     23          3.20     " 

0.  I 

5-5 

5-6 

50 

0.  I 

4.8        4-9 

83 

"   23        3.30    " 

O.  I 

5-3 

5-4 

49 

0.2 

4.0        4.2 

75 

"    23       3.40    " 

0.3 

7.0 

7-3 

66 

O.  I 

4-5        4-6 

82 

"   23 

3.50        " 

0.  I 

IO.O 

IO.I 

90 

0.2 

5.0        5.2 

93 

Direction   of  How  of   electric   current 

"   23 

4.10        " 

0.6 

4.0 

4.6 

4i 

O.O 

I.O           I.O 

18 

reversed  in  both  cells  at  4.00  I'.M. 

"   23 

4.20        " 

0.5 

4.0 

4-5 

40 

Trace 

Trace 

O.I 

2 

"   23 

4.30        " 

''•3 

4-5 

4.8 

43 

0.  I 

Trace 

0.  I 

2 

"   23 

4.40        " 

0.3 

4-3 

4.6 

41 

O.I 

0.2 

2.  I 

5 

..      23 

4-5"     " 

o-3 

5-2 

5-5 

49 

0.0    |       I.O 

I.O 

IS 

. 

23 
"      23 

5.OO 

5.io     " 

0.2 

5-2 

IO.O 

5-4 

10.2 

49 
48 

O.I 

3-5 

3-f> 

34 

and    0.038  ampere-hour  per  gallon 

"      23 

5.20     " 

O.I 

9.8 

9-9 

47 

0.3 

4.0 

4-3 

41 

in  cells  Nos.  i  and  3  respectively. 

"      23 

5.30     " 

O.2 

it  .0 

II.  2 

53 

O.  I 

3-8 

3-9 

37 

Current  shut  off   and  cells  drained  at 

5-45  I'-M. 

"      24 

.15   A.M.              O.O 

4-5 

4-5 

21 

0.3 

1-5 

1.8        17 

Began   operations   at   11.10  A.M.  with 

"      24 

.25     "       !     o.o 

6.5 

6-5 

31 

o.i        3.5 

3-6        34 

conditions  unchanged. 

"      24 

•  35      " 

0.0 

7-0 

7.0 

33 

o.i        4.0 

4-1        39 

"      24 

•45      ' 

0.0 

7-5 

7-5 

35 

o.i        4.1 

4-2        4° 

"      24 

•55      ' 

0.3 

9-5 

9.8 

46 

0.3 

5-2 

5-5        52 

"   24 

.12   P.M. 

0.0 

o.o 

o.o 

47 

O.  I 

6.0 

6.1 

57 

"   24 

.25       " 

0.2 

2.O    !       2.  2 

58 

O.  2 

6.0 

6.2 

58 

"   24 

.40       " 

0-3 

2.0 

2.3 

58 

O.2 

6.0 

6.2    |       58 

!.'  24 

•55       ' 

0.0 

I.O 

1  .0 

52 

O.O 

6.0 

(>.o  ;     57 

24 

.  IO 

0.0 

2.O 

2.0 

57 

O.O 

5.0 

5.0        47 

"   24 

.25     " 

o. 

2-5 

2.6 

59 

0.2 

4.8 

5-0        47 

'.!  24 

•45      ' 

o. 

2.2 

2-4 

58 

O.I 

4.8 

4-9  '     4(> 

24 

•55     ' 

o. 

2.2 

2.2 

58 

0.  I 

4.8 

4.9        46 

"  24 

.10     " 

0. 

2.2 

2-4 

58 

O.  I 

5  -O 

5.1        48 

"  24 

•  25     " 

o. 

2.2 

2.4 

58 

O.I 

5-5 

5-6  ,      53 

"  24 

.40     " 

o. 

3-o 

3-2 

52 

0.2 

5-0 

5-2   ;     40 

• 

"  24 

•55      ' 

o. 

2.O 

2.2 

58 

O.2 

5-o 

5-2 

49 

"  24 

3.10     " 

o. 

1-5 

1.6 

55 

O.  I 

5-2 

5-3 

50 

"  24 

3-25     ' 

o. 

I.O 

I.I 

52 

O.  I 

5-0 

5-i 

48 

"  24 

3-40     " 

o. 

1  .0 

I  .  I 

52 

O.2 

4.8 

5-0 

47 

"  24 

3-55     ' 

o. 

I.O 

I  .  I 

52 

O.  I 

5-0 

5-1 

48 

"  24 

4.10     " 

o. 

o-5 

0.6 

50 

O.I 

5-0 

5-i 

48 

"  24 

4-25     ' 

o. 

0.5 

0.6 

50 

O.  I 

5-0 

5-i 

48 

"  24 

4.40     " 

o. 

0.5 

0.6 

50 

O.  I 

5-0 

5-  1 

48 

"  24 

4-55      ' 

o. 

0.5 

0.6 

50 

O.I 

4.8 

4-9 

46 

"  24 

5.10     " 

0. 

o.o 

O.I 

48 

O.  I 

5-o 

5-i 

48 

"  24 

5-25     ' 

o.o 

0.0 

0.0 

47 

o.o 

5.0 

5-0 

47 

"  24 

5.40     " 

O.  I 

0.0 

O.I 

48 

0.0 

6.0 

6.0 

56 

Current    shut    off    and    cells    drained 

at  5.45  I'.M. 

SUMMARY  AND   DISCUSSION   OF  DATA     OF  1807. 


CONDITIONS    OF    OXIDATION    AND    AMOUNTS    OF    ELECTROLY TICALLY    DECOMPOSED    IRON 
LEAVING    THE    CELLS.  —  Concluded. 


Cell 

Cell 

No.  3 

Due. 

1897. 

Hour. 

P;ir 

Is  per  M 

lion. 

-'£? 

Par 

s  per  M 

Ilion. 

^H  " 

Remarks. 

T 

u  y  £  ~ 

TV.nl 

U  ,.  t  : 

Iron 

Iron. 

£•  - 

Iron. 

0. 

Began    operations    at    7.00  A.M.    with 

July  26 

g.IO  A.M. 

1      O.O 

9.0 

9.0 

42 

O.O 

4.0 

4-0 

38 

conditions  unchanged. 

"    26 

g.25       " 

i      O.O 

8.5 

8-5 

40 

0.0 

3-5 

3-5 

33 

"    26 

9.40      " 

0.6 

9.0 

9.6 

45 

0.7 

4.0 

4-7 

I     44 

'    26 

9-55      ' 

0.0 

9-5 

9-5 

45 

O.O 

4-0 

4-0 

38 

'    26 

IO.IO       " 

0.2 

9-5 

9-7 

46 

0.2 

4-5 

4-7 

44 

'    26 

10.25     " 

O.I 

IO.O 

10. 

48 

O.  I 

4-5 

4.6 

43 

'    26 

o.  40     '  ' 

O.I 

10.  I 

10. 

48 

O.I 

5-0 

5-1 

48 

'      26 

0-55      " 

O.  I 

IO.O 

IO. 

48 

0.0 

6.0 

6.0 

57 

'      26 

I.  10        " 

0.  I 

IO.O 

10. 

48 

O.O 

5-0 

5-0 

47 

'      26 

1.25     " 

O.I 

9-5 

9-  * 

45 

0.0 

5-0 

5-0 

47 

'      26 

2.55    P.M. 

0.  I 

IO.O 

IO. 

48 

O.  I 

5.0 

5-1 

48 

"      26 

1.  10      " 

O.  I 

IO.O 

10. 

48 

O.O 

5-0 

5-o 

47 

'      26 

1.25       " 

0.  I 

.9-5 

9- 

45 

O.O 

5.0 

5-0 

47 

'      26 

1.40      " 

0.  I 

IO.O 

IO. 

48 

O.  I 

5-1 

5-2 

48 

•     26 

i-55     ' 

O.  I 

IO.O 

10. 

48 

O.  I 

5-1 

5.2 

48 

'      26 

2.25     " 

O.O 

IO.O 

IO.O 

47 

O.  1 

5-i 

5-2 

48 

'      26 

2-55      " 

0.0 

IO.O 

IO.O 

47 

O.  I 

5.1 

5-2 

48 

'      26 

3-25     ' 

O.O 

IO.O 

IO.O 

47 

O.O 

5.0 

5-0 

47 

"      2f) 

3-55      ' 

0.0 

IO.O 

IO.O 

47 

0.0 

5-o 

5-0 

47 

"      26 

4.25      ' 

0.0 

IO.O 

IO.O 

47 

O.O 

5-0 

5-0 

47 

"     26 

4-55     ' 

O.O 

9-5 

9-5 

45 

0.0 

4-5 

4-5 

42 

"     26 

5.25     ' 

0.0 

IO.O 

IO.O 

47 

0.0 

5.0 

5.o 

47 

Ran  continuously  over  night. 

"     27 

9.05  A.M. 

O.O 

IO.O 

IO.O 

47 

0.0 

7-5 

7-5 

7i 

"      27 

9.15       " 

O.O 

IO.O 

IO.O 

47 

O.O 

7.0 

7.  o 

66 

"      27 

1.  15       ' 

0.0 

IO.O 

IO.O 

47 

2.0 

5-o 

7-° 

66 

"    27 

1.30       " 

O.O 

9.0 

9.0 

42 

2.0 

5-5 

7-5 

71 

"   27 

1-45     " 

O.O 

IO.O 

IO.O 

47 

2.O 

5  o 

7-o 

66 

"   27 

2.OO  M. 

0.3 

II.  0 

11.3 

53 

4.0 

6.0 

IO.O 

94 

"     27 

2.45    P.M. 

O.O 

IO.O 

IO.O 

47 

4-o 

5-o 

9.0 

85 

"     27 

1.  00       " 

o.5 

IO.O 

10.5 

50 

6.0 

8.0 

14.0 

132 

"   27 

I.I5       ' 

0.0 

6.0 

6.0 

28 

1.0 

7-0 

8.0 

75 

"  27 

I.JO       " 

O.O 

5-o 

5.0 

24 

1.0 

6-5 

7-5 

71 

Ian  continuously  over  night. 

"  28 

9.15  A.M. 

0.0 

6.0 

6.0 

28 

O.O 

5-0 

5-0 

47 

"   28 

9.25       " 

O.O 

7.0 

7-0 

33 

0.0 

5-o 

5-0 

47 

"  28 

9-35     " 

0.0 

6.0 

6.0 

28 

0.0 

5.0 

5-o 

47 

"      28 

9-45     ' 

0.0 

6.0 

6.0 

28 

O.O 

4.0 

4.0 

38 

"   28 

9-55     " 

O.O 

5-0 

5-0 

24 

0.0 

4o 

4-5 

42 

hut  down  from  10.00  A.M.  to  3.00  P.M. 

"      28 

3.10   I'.M. 

0.0 

9.0 

9.0 

42 

O.2 

7-0 

7-2 

68 

and   cleaned    scale    and    mud    from 

"   28 

3-40      " 

O.O 

9-5 

9-5 

45 

0.0 

6.0 

6.0 

57 

electrodes  No.  I. 

"  28 

4.10      " 

0.0 

9.0 

9.0 

42 

0.0 

6.0 

6.0 

57 

direction  of  flow   of  electric   current 

"   28 

4-30      " 

O.O 

9.0 

9.0 

42 

O.  I 

3-O 

3-1 

29 

reversed  in  both  cells  at  4.15  P.M. 

"      28 

4  40     " 

0.3 

9.0 

9-3 

44 

0.  I 

2.5 

2.6 

25 

"  28 

5.10     " 

0.5 

9.0 

9-5 

45 

0.2 

2-5 

2-7 

25 

of  the  positive  plates  (equal  to  one  side  of  all 
plates)  of  set  No.  i  was  1510  square  inches, 
and  the  area  of  the  electrolyte  was  1300 
square  inches.  In  set  No.  2  the  correspond 
ing  figures  were  3320  and  3170,  respectively. 
A  potential  difference  of  1.5  volts  was  main 
tained  on  set  No.  i,  and  of  i.o  volt  on  set 
No.  2.  From  10.00  A.M.  to  2.00  P.M.,  Sept.  30, 
set  No.  i  was  operated  at  a  potential  differ 
ence  of  3.5  volts.  The  rate  of  flow  of  water 


was  maintained  uniformly  throughout  the 
first  run  at  0.5  cubic  foot  per  minute  through 
each  cell,  and  determinations  were  made  every 
two  hours  of  the  amounts  of  iron  in  the  water 
as  it  left  the  cells.  During  this  run  the  elec 
tric  current  was  held  uniformly  at  6.0  am 
peres.  On  the  second  run  the  strength  of 
electric  current  averaged  15  amperes.  The 
rate  of  How  of  water  was  i.o  cubic  foot  per 
minute. 


402 


WATER   PURIFICATION  AT  LOUISVILLE. 


The  results  of  the  determinations  of  the 
amounts  of  iron  in  the  water  as  it  left  the  cells, 
and  the  percentages  which  these  amounts 
were  of  the  theoretical,  are  given  in  the  next 
table. 

During  the  first  run  the  gas  evolved  in  cell 
No.  i  appeared  to  be  almost  constant  in 
amount.  In  cell  No.  2  almost  no  gas  was 
observed  up  to  6.30  A.M.,  Sept.  29.  From 
this  time  the  formation  of  gas  steadily  in 
creased  in  amount  till  at  the  close  of  the  run 
there  was  nearly  as  much  gas  being  formed 
in  No.  2  as  in  No.  i. 

On  examination  the  positive  plates  of  set 
No.  2  were  found  to  be  covered  with  a  heavy 
coating  of  what  appeared  to  be  an  irregularly 
hydrated  form  of  red  oxide,  somewhat  granu 
lar  in  form.  In  the  bottom  of  this  ce'l  was 
found  a  heavy  accumulation  of  red  oxide, 
green  hydrate,  and  scale. 

TABLE  SHOWING  THE  AMOUNTS  OF  IRON 
LEAVING  THE  TWO  CELLS  CONTAINING 
STEEL  ELECTRODES  ON  WHICH  POTENTIAL 
DIFFERENCES  OF  1.5  AND  1.0  VOLTS,  RESPEC 
TIVELY,  WERE  MAINTAINED. 


Date. 

1897. 

Hour. 

Cell  No.  1—1.5  Volts. 

Cell  No.  2—1.0  Volt. 

Water. 

Parts  per 
Million. 

Per    Cent 
of  the 
Theoreti 
cal. 

Water. 
Parts  per 
Million. 

Per   Cent, 
of  the 
Theoreti 
cal. 

Sept.  28 

2.00   I'.M' 

S.O 

no 

6.4 

88 

'•       28 

3.00     " 

7-5 

tor 

5-2 

7i 

"       28 

5.OO     " 

9.3 

134 

7-2 

98 

"       23 

y.OO    " 

8.0 

1  08 

5-3 

72 

"     28 

9.00    " 

5-3 

79 

6.5 

89 

"     28 

11.00    " 

6.0 

82 

7.0 

95 

"      29 

I.OO  A.M. 

6.3 

86 

7-4 

IOO 

"     29 

3.OO     " 

8.0 

108            6.5 

38 

;     29 

5  .  OO     " 

6.0 

81            6.0 

Si 

"     29 

7-OO     " 

5-8 

79            7-3 

99 

'     29 

9.OO     " 

9.0 

122                 5-8 

78 

29 

1  1.  00     " 

8.0 

I  08             6.1 

S3 

"       29 

i.oo  r.M. 

6.1 

83             5-8 

78- 

"     29 

3.00  " 

5-9 

80             6.3 

85 

;     29 

5-oo   " 

5-2              70            5-7 

77 

"       29 

7.00    " 

5.9              So            6.4 

86 

29 

9.00    " 

6.2 

84 

5.8 

73 

29 

II.  OO    " 

7-9 

107 

6.1 

83 

"         30          1.  00  A.M. 

7-8 

105             5  •  6 

77 

30    ,      3.00     " 

6.7 

91             5-7 

77 

30          5.00     " 

6.6 

89     i        5-8 

73 

30 

7.00    " 

6.7 

91 

8-3 

112 

"         30 

9.00    " 

6.7 

91 

S.o 

108 

Averages 
Increased  voltage  on 

6.8 
No.  i,  t 

92            6.2            84 
->  3.5  am    stopped  No.  2. 

Sept.  30 

1       30 

1  l.uu  .'i.m. 
I.OO    I'.M. 

II-5 

[0.8 

118 

30 
30 

1.30 
2.OO     " 

s's 

93 

It  will  be  seen  that  the  amounts  of  iron 
leaving   cell    No.    i    were   somewhat   greater 


than  in  the  case  of  cell  No.  2,  the  averages 
being  92  and  84  per  cent,  of  the  theoretical 
rate,  respectively. 

A  slight  increase  in  the  amount  of  iron 
leaving  the  cell  was  noticed  after  increasing 
the  voltage  and  current  in  No.  i,  but  as  this 
soon  returned  to  the  normal  it  was  con 
cluded  that  the  first  high  results  were  due  to 
the  effect  of  the  increased  volume  of  water 
and  electric  current  removing  the  metal  pre 
viously  decomposed,  from  the  plates  and  por 
tions  of  the  cell  upon  which  they  had  lodged. 

It  was  evident  from  these  experiments  that 
iron  could  be  decomposed  at  a  potential  dif 
ference  as  low  as  i.o  volt,  and  that  gas  was 
formed  in  the  process. 

There  was  some  indication  that  the  higher 
potential  was  slightly  more  efficient  than  the 
lower,  but  the  differences  were  not  great 
enough  to  make  certain  that  differences  in 
arrangement  of  supporting  framework  under 
the  electrodes,  or  slight  variations  in  the  dis 
placement  of  the  water  in  the  cells,  were  not 
the  explanation  of  these  results.  To  make 
this  point  clear  new  electrodes  were  prepared 
of  the  same  metal,  and  river  water  treated  at 
10,  5,  2.5,  1.75,  and  1.5  volts  difference  in 
potentials,  respectively.  Each  experiment 
was  continued  to  the  equivalent  of  0.05  am 
pere-hour  per  gallon  of  treated  water  and  the 
amounts  of  iron  were  determined.  Within 
the  limits  of  accuracy  no  difference  could  be 
found  in  the  rate  of  hydrate  formation  at  the 
several  potential  differences. 

It  was  therefore  concluded  that  potential 
differences  between  the  limits  of  i.o  and  220 
volts  exerted  no  apparent  influence  on  the 
rate  of  formation  of  hydrate;  that  scale  and 
gas  formed  with  apparently  the  same  rapidity 
at  all  potential  differences;  and  that  the  prac 
tical  limits  of  construction  with  references 
to  the  area  of  electrode  surface  and  length 
of  electrolyte  would  be  the  controlling  factors 
in  determination  of  the  potential  difference  to 
employ  in  practice. 

Influence  on  tltc  Formation  of  Hydrate  of  Cur 
rent  Density. 

The  current  density  ranged  from  0.30  to 
2.08  amperes  per  square  foot  of  active  elec 
trode  surface  during  these  tests.  For  the 


SUMMARY  AND   DISCUSSION   OF  DATA    OF  1801 


4°3 


most  part  it  was  about  1.04  amperes  with  the 
large  devices.  In  the  case  of  some  labora 
tory  experiments  a  current  density  as  high  as 
50.4  amperes  per  square  foot  was  employed 
at  times,  but  the  usual  density  was  about  15 
amperes  per  square  foot. 

In  connection  with  the  low  potential  experi 
ment  described  above,  current  densities  as  low 
as  0.26  ampere  per  square  foot  were  em 
ployed. 

Within  these  limits  no  marked  influence  of 
current  density  upon  the  formation  of  hydrate 
was  noticed,  but  it  is  probable,  as  noted 
above,  that  the  deposition  of  iron  at  the  nega 
tive  pole  was  somewhat  greater  with  the  high 
than  with  the  low  densities,  though  the  in 
creased  rapidity  of  replacement  of  electrolyte 
due  to  increased  flow  of  water  through  the 
cells  would  probably  compensate  for  this  in 
a  measure.  Theoretically,  as  has  been  ex 
plained  above,  the  lower  the  current  density 
the  lower  the  rate  of  deposition  of  metal  on 
the  negative  pole.  Current  density  as  low 
as  admissible  with  economic  construction  of 
cells  should  therefore  be  employed. 

Influence  on  the  Formation  of  Hydrate  of  the 
Composition  of  the  Iron. 

The  rolled  wrought-iron  plates  used  in  this 
work  were  of  the  following  percentage  com 
position: 

Carbon 0.06 

Silica 0.28 

Sulphur 1.58 

Phosphorus o.  14 

Manganese o.oo 

Iron 97-94 

So  far  as  was  learned  the  only  way  in  which 
the  composition  of  the  iron  might  affect  the 
formation  of  hydrate  was  indirectly  through 
its  effect  upon  the  passivity  of  the  metal  to 
the  acid  ions  of  the  water.  This  subject  has 
been  dealt  with  above  in  connection  with  pas 
sivity,  when  it  was  stated  that  no  difference 
in  hydrate  formation  was  apparent  in  the  va 
rious  grades  of  metal  used  here,  which  were 
clearly  due  to  differences  in  the  composition 
of  the  several  irons  and  steel. 

From  a  practical  point  of  view  the  differ 
ences  in  passivity  of  electrodes  due  to  varia 


tions  in  the  composition  of  the  metal  would, 
under  the  conditions  of  these  tests,  have  been 
almost  completely  disguised  by  the  acquired 
passivity  caused  by  coatings  of  iron  oxide. 


Directly,  the  composition  of  the  river  water 
influences  the  formation  of  hydrate  princi 
pally  through  the  action  of  the  atmospheric 
oxygen  dissolved  in  the  water  in  converting 
the  iron  into  the  insoluble  ferric  hydrate. 
This  action  is  a  very  important  one.  It  is 
also  probable  that  the  suspended  matter 
affects  the  character  of  the  surface  coatings 
especially  on  the  negative  electrode. 

Indirectly,  the  relative  amounts  of  the  dif 
ferent  acid  ions  in  the  river  water  influence 
the  formation  of  hydrate  through  their  dif 
ferent  relations  to  the  passivity  of  the  iron. 
In  connection  with  the  current  density,  also, 
the  composition  of  the  river  water  is  a  factor 
in  the  consideration  of  deposition  of  metallic 
iron  on  the  cathode.  The  last  two  points  are 
referred  to  in  detail  at  the  beginning  of  this 
section. 

Influence  on  the  Formation  of  Hydrate  of  Re 
versing  the  Direction  of  the  Electric  Current. 

When  the  direction  of  flow  of  the  electric 
current  passing  through  the  electrodes  and 
electrolyte  is  reversed,  the  positive  electrode 
(which  was  previously  the  negative)  is  at  the 
outset  saturated  with  hydrogen  gas  and  the 
surface  is  coated  with  metallic  iron,  probably 
mixed  somewhat  with  suspended  matters 
from  the  water.  Comparison  in  the  last  set 
of  tables  of  the  amount  of  iron  in  the  water  as 
it  left  the  cells  before  and  after  reversals  of 
current  on  July  23  at  4.00  P.M.,  and  on  July 
28  at  4.15  P.M.,  shows  that  in  three  of  the 
four  instances  the  rate  of  decomposition  c:f 
iron  suffered  a  marked  diminution  for  more 
than  an  hour.  The  cause  of  this  is  not  clear',  y 
understood,  but  it  appears  to  be  associated 
with  the  occluded  hydrogen  in  the  pores  of 
the  metal  and  with  the  surface  coatings,  which 
will  vary  of  course  with  the  frequency  of  re 
versal  and  the  character  of  the  river  water. 
In  practice  these  marked  diminutions  in  the 


WATER  PURIFICATION  AT   LOUISVILLE. 


formation  of  hydrate  would  be  a  serious  mat 
ter  and  for  a  time  would  require  the  opera 
tion  of  a  reserve  portion  of  the  plant,  both 
with  regard  to  the  cells  and  the  generating 
appliances. 


When  the  electric  current  was  shut  off 
from  the  electrodes  and  the  cells  kept  full  of 
water  it  was  repeatedly  noted  that  the  decom 
position  of  iron  and  formation  of  gas  continued 
for  a  long  time.  This  was  due  to  a  galvanic 
action,  the  metal  being  electro-positive  to  the 
surface  coating  of  oxide.  During  the  month 
of  April  and  early  part  of  May,  when  the  elec 
trical  devices  were  out  of  service  on  numer 
ous  occasions  while  tests  with  chemicals  were 
being  made,  it  is  estimated  that  the  total 
weight  of  the  electrodes  decreased  65  pounds, 
due  to  this  factor  alone.  On  the  grounds 
of  economy  and  of  comparable  conditions  for 
reliable  data,  it  became  necessary  to  drain  the 
water  from  the  cells  as  soon  as  the  electric 
current  was  stopped.  So  far  as  is  known  the 
subsequent  formation  of  hydrate,  when  the 
electric  current  was  applied  following  a  pe 
riod  of  rest  in  which  the  electrodes  were  cov 
ered  with  water,  was  not  seriously  influenced 
by  this  procedure,  which,  however,  for  the 
reasons  stated  above,  was  found  to  be  imprac 
ticable. 

After  the  first  of  June  the  water  was 
drained  out  of  the  cells  as  soon  as  the  current 
was  turned  off.  In  consequence  of  the  action 
of  the  air  it  was  found  that  the  rusting  of  the 
electrodes  thus  produced,  increased  the  ac 
quired  passivity  of-  the  iron,  and,  when  the 
electrodes  were  again  put  in  service,  the  rate 
of  formation  of  hydrate  was  abnormally  low 
for  a  time.  This  is  shown  in  the  tab'e  on  page 
400  by  the  results  on  the  morning  of  July  24, 
when,  following  a  rest  after  draining  the  cells, 
of  about  41  hours,  the  electrodes  did  not  yield 
the  normal  amount  of  iron  for  half  or  three- 
quarters  of  an  hour.  In  other  cases,  where 
the  period  of  rest  was  longer  the  evidence 
shows  a  more  prolonged  diminution  in  the 
rate. 


Per  Cent,  of  Metal  Wasted  in  this  Process. 

When  the  potential  difference  of  the  cur 
rent  between  adjoining  plates  was  3  volts  or 
more  the  evidence  showed  a  rate  of  decompo 
sition  of  iron  on  the  positive  plate  equivalent 
to  about  100  per  cent,  of  the  theoretical  rate 
of  1.05  grams,  or  16.2  grains  per  ampere-hour. 
Of  this  iron  an  amount  equivalent  to  about 
10  per  cent,  of  the  theoretical  rate  was  found 
deposited  on  the  negative  plate.  The  amount 
of  iron  leaving  the  cell  in  the  form  of  avail 
able  hydrate  seemed  to  vary  considerably,  but 
averaged  about  40  per  cent,  of  the  theoretical 
rate.  Taking  into  consideration  the  fact  that 
eventually  the  plates  become  too  thin  for  use 
and  have  to  be  discarded,  it  seems  fair  to  con 
clude  that  in  this  process  of  producing  iron 
hydrate  substantially  one-half  of  the  metal  is 
wasted  by  passing  into  the  water  in  the  form 
of  non-hydrated  and  non-available  scales  of 
iron  oxide. 

The  experiments  of  Sept.  28  to  30  indicate 
that  no  substantial  advantage  in  this  respect 
would  be  obtained  with  potential  differences 
as  low  as  i  volt. 

Resistance  to  the  Passage  of  Electric  Current  of 
Films  of  Iron  Oxide. 

The  results  of  analyses  and  of  observations 
of  scales  in  the  water  leaving  the  cells  showed 
that  the  films  of  iron  oxide  attached  to  the 
positive  electrodes  remained  there  only  tem 
porarily,  and  came  off  at  an  irregular  rate 
from  time  to  time.  In  consequence  thereof 
it  is  not  probable  that  the  entire  surface  was 
covered  at  any  one  time,  in  the  course  of 
regular  operations,  with  a  film  which  very 
materially  increased  the  resistance  of  the  elec 
trodes.  Compared  with  new  metal  the  plates 
doubtless  offered  a  certain  resistance,  but 
within  the  ranges  of  service  to  which  these 
electrodes  were  subjected  the  increase  in  re 
sistance  was  within  the  limits  of  observation, 
or  less  than  I  volt  at  400  amperes  or  .0025 
ohm. 

Percentage  of  Electric  Power   Wasted  in   this 
Process. 

Under  the  above-described  conditions  of 
operation,  with  potential  differences  between 


SUMMARY  AND   D1SCUSSJON  OF  DATA    OF  18'J7. 


4°5 


the  electrodes  of  3  volts  or  more,  the  evidence 
shows  that  between  50  and  60  per  cent,  of  the 
electric  current  was  wasted  in  removing  iron 
in  the  form  of  scales,  due  to  the  formation  of 
oxygen  at  the  surface  of  the  plates,  and  in 
depositing  some  of  the  available  metal  upon 
the  negative  electrodes.  This  does  not  in 
clude  the  effect  of  scales  in  offering  increased 
resistance  to  the  electric  current,  as  noted  in 
the  last  paragraph.  Combining  the  three 
items,  the  waste  of  electric  power  may  be 
safely  placed  at  60  per  cent. 

The  experiments  of  Sept.  28  to  30  with  po 
tential  differences  as  low  as  i  volt  indicate 
that  there  is  no  reason  under  these  conditions 
for  modifying  the  above  figures. 

Influence  of  this  Process  on  Subsidence  and  Fil 
tration. 

Comparing  the  effect  of  this  process  upon 
the  efficiency  of  subsidence  and  nitration  of 
water  with  that  of  chemical  treatment  such 
as  persulphate  of  iron  or  sulphate  of  alumina. 
when  the  degree  of  coagulation  is  the  same, 
it  is  to  be  pointed  out  that  under  the  condi 
tions  tested  the  hydrogen  gas  evolved  at  the 
cathode  has  a  slight  effect  in  retarding  sub 
sidence,  and  also  at  times  reduces  the  length 
of  run  between  washings  of  the  filter  by  plug 
ging  up  some  of  the  pores  of  the  sand  layer. 

Compared  with  aluminum  the  iron  elec 
trodes  offer  much  less  difficulty  with  gas  for 
mation  when  equal  coagulation  is  obtained. 
Some  laboratory  observations  in  May  showed 
that  the  ratio  of  gas  formed  by  equivalent  co 
agulation  with  aluminum  and  iron  electrodes 
was  about  2  to  i.  In  practice  as  the  elec 
trodes  become  covered  with  scale  this  ratio 
is  greatly  increased.  Thus  the  ratio  of  gas 
formation  with  aluminum  and  iron  electrodes 
after  long  service  in  connection  with  the  filter, 
and  under  the  same  conditions  other  than  the 
surface  coatings,  was  found  on  June  8  to  be 
i  ^o  to  4.  It  is  to  be  noted  that  these  ratios 
refer  to  amounts  of  evolved  gas.  As  the 
amount  required  to  saturate  the  water  formed 
different  percentages  of  the  total,  the  ratios 
are  not  absolutely  exact. 

Influence  of  the  Process  on  the  Composition  of 
Filtered  Water. 

Like  all  electrolytic  processes  of  this  gen 


eral  type,  the  iron  process  does  not  add  to  the 
filtered  water  any  mineral  acid  to  make  the 
water  less  desirable  when  used  in  boilers,  and 
it  does  not  add  to  the  water  any  free  carbonic 
acid  to  affect  corrosion.  In  addition  to  the 
ordinary  removal  of  suspended  mineral  and 
organic  matters  and  a  slight  removal  of  dis 
solved  organic  matter,  however,  it  removes 
the  atmospheric  oxygen  in  the  water  in 
amounts  proportional  to  the  iron  obtained  as 
hydrate.  Up  to  a  certain  point  this  factor  is 
of  little  practical  significance,  but  when  the 
process  is  carried  to  a  degree  where  the  oxy 
gen  is  all  or  nearly  all  used  for  this  purpose 
there  is  danger  of  some  of  the  iron  passing 
into  the  filtered  water.  A  filtered  water  con 
taining  no  oxygen  would  also  be  undesirable 
in  several  ways.  Up  to  a  certain  point,  there 
fore,  this  process  can  be  used  with  satisfaction 
so  far  as  composition  of  the  filtered  water  is 
concerned.  Beyond  this-  point  (exhaustion 
of  atmospheric  oxygen)  the  application  of 
this  process  is  inadmissible. 


From  the  evidence  presented  in  this  section 
it  may  be  concluded: 

1.  Under  practical  conditions  this  process 
can    be    used    to    produce    ferric    hydrate,    a 
good  coagulant,  up  to  the  point  where  the 
atmospheric  oxygen  dissolved  in  the  water  is 
not  completely  exhausted. 

2.  The  evolution  of  gas  is  fairly  small,  com 
paratively  speaking,  but  the  indications  were 
that  at  times  the  gas  might  exert  a  retarding 
influence    upon    subsidence    and    a    clogging 
effect  upon  filters. 

3.  The  rate  of  production  of  ferric  hydrate 
was  reasonably  uniform  at  its  minimum  limit, 
except  for  periods  in  the  vicinity  of  one  hour 
following  a  reversal   of  the  direction  of  the 
current  and  an  exposure  of  the  plates  to  the 
atmosphere. 

4.  Owing    to    galvanic    action    when    the 
coated  plates  were  allowed  to  remain  in  water 
when  out  of  service,  the  loss  of  metal  made  it 
imperative  to  avoid  this  procedure  except  for 
very  short  intervals. 

5.  Under  conditions  of  good  practice  the 
amount  of  metal  wasted  as  oxide  scale  would 
be  substantially  50  per  cent. 


406 


WATER   PURIFICATION  AT  LOUISVILLE. 


6.  Under  conditions  of  good  practice  the 
amount  of  power  wasted  would  reach  about 
60  per  cent. 

SECTION  No.  5. 

DETAILED  ACCOUNT  OF  THE  ELECTROLYTIC 

FORMATION   OF  ALUMINUM   HYDRATE 

IN  THE  OHIO  RIVER  WATER. 

During  the  latter  part  of  1896  and  first  part 
of  1897,  several  factors  operated  together  to 
bring  forward  again  the  process  of  the  forma 
tion  of  a  coagulant  by  the  electrolytic  decom 
position  of  metallic  aluminum.  As  was 
explained  at  the  close  of  Chapter  XI 1,  inves 
tigations  in  July  and  August,  1896,  led  to  the 
conclusion  that  the  use  of  electrolytically  pre 
pared  aluminum  hydrate  was  out  of  the  ques 
tion  because  of  its  excessive  cost,  but  that  the 
use  of  an  electrolytically  prepared  coagulant 
presented  certain  distinct  advantages  over  the 
use  of  sulphate  of  alumina.  Chief  among  the 
factors  which  led  to  further  consideration  of 
this  process  were  the  following: 

1.  The    operations    with    iron     electrodes 
showed  clearly  that  potential  differences  very 
much    lower    than    those    employed    during 
July  and  August,  1896,  could  be  used  in  this 
general  process  with  equally  satisfactory  re 
sults,    thus    greatly    decreasing    the    cost    of 
power. 

2.  The  cost  of  metallic  aluminum  had  de 
creased  to  about  one-half  its  cost  in  August, 
1896. 

3.  It    appeared    that    the    electric    current 
gave  results  nearly  twice  as  effective  when 
new  aluminum  electrodes  were  used  as  when 
iron    plates    were    employed.     This    was    of 
much   practical   significance  in  consideration 
of   the    construction    and    maintenance    of    a 
plant. 

4.  President  Long  requested  that  the  pro 
posed  investigations  of  coagulants  be  made  as 
full  and  thorough  as  consistent  with  the  prac 
ticability  of  the  results  obtained. 

For  these  reasons  the  use  of  electrolytically 
prepared  aluminum  hydrate  was  again  given 
attention  in  connection  with  other  coagulants. 

Early  in  the  course  of  the  investigations  it 
was  found  that  aluminum  in  the  form  of  elec 
trolytically  prepared  hydrate  was  no  more 


effective  than  when  in  the  form  of  hydrate 
obtained  from  the  decomposition  of  the  sul 
phate  by  the  lime  in  the  river  water.  It  was 
also  seen  that  the  efficiency  of  aluminum 
plates  in  practice  was  very  much  less,  both  in 
amount  and  in  regularity,  than  was  indicated 
to  be  the  case  by  the  results  with  new  plates. 

It  seemed  inadvisable,  therefore,  to  make 
the  study  of  the  details  of  this  process  as  ex 
haustive  as  those  of  the  formation  of  iron  hy 
drate  electrolytically,  although  in  the  main 
the  investigations  of  both  processes  were  car 
ried  on  simultaneously.  The  following  ac 
count,  while  it  covers  the  bulk  of  the  ground 
fully  investigated  in  connection  with  iron 
electrodes,  is,  accordingly,  not  as  complete  as 
the  investigation  in  the  case  of  iron  as  re 
corded  in  section  Xo.  4;  and,  furthermore, 
owing  to  the  peculiar  and  widely  varying  re 
sults,  it  has  been  necessary  in  some  instances 
in  order  to  account  for  certain  observations 
to  introduce  explanations  and  theories,  as  an 
exhaustive  study  of  these  points  was  not  war 
ranted  by  the  available  time  and  the  imprac 
ticability  of  the  process. 

The  same  general  plan  as  was  employed  in 
the  presentation  of  the  investigations  of  the 
iron  process  is  followed  here. 


As  has  been  presented  in  the  general  dis 
cussion  of  the  process  of  decomposition  of 
metals  under  the  action  of  an  electric  current, 
the  percentage  of  the  acid  ions  which  attacks 
and  decomposes  water  may  be  stated  to  repre 
sent  the  degree  of  passivity  of  the  electrodes, 
on  the  assumption  that  when  an  electrode  is 
perfectly  non-passive  (completely  active),  all 
of  the  acid  ions  attack  the  plate  and  no  water 
is  decomposed  at  the  anode. 

The  principal  points  learned  in  regard  to 
the  action  of  the  acid  ions  upon  aluminum 
electrodes,  so  far  as  it  was  considered  prac 
ticable  to  investigate  the  subject,  were  as  fol 
lows  : 

i.  The  fact  that  in  all  cases  within  the  lim 
its  employed  a  gas  appeared  to  be  liberated 
at  the  positive  pole  when  aluminum  elec 
trodes  of  bright  metal  were  used  in  electro 
lytes  formed  of  pure  solutions  of  each  of  the 
several  acid  ions  normally  present  in  the  Ohio 


SUMMARY  AND   DISCUSSION   OF  DATA    OF  1897. 


407 


River  water,  indicates  that  aluminum  is  nor 
mally  passive  to  all  of  these  ions  to  a  certain 
but  variable  degree. 

2.  Aluminum  seems  to  be  most  passive  to 
the  ions  of  nitric  acid.     This  would  be  ex 
pected  from  the  fact  that  aluminum  is  not 
readily  soluble  in  nitric  acid. 

3.  The    acquired    passivity    of    aluminum 
electrodes,  that  is,  the  passivity  due  to  the 
formation  of  a  coating  of  oxide  on  the  face 
of  the  plates,  continually  increases  in   prac 
tice;   and  while  it  fluctuates  somewhat,  due  to 
the  scaling  of  the  plates,  there  is  strong  evi 
dence  to  indicate  that  after  considerable  ser 
vice    the    rate    of   formation    of   the    hydrate 
might  decrease  to  almost  nothing  on  this  ac 
count. 

It  is  to  be  noted  in  this  connection  that  the 
metallic  aluminum  used  during  these  inves 
tigations  was  the  very  best  grade  of  commer 
cial  rolled  plate.  How  far  this  may  have 
affected  the  results  is  difficult  to  say,  but  the 
indications  are  that  a  less  pure  grade  of  metal 
might  be  more  readily  soluble,  although  pos 
sibly  no  more  efficient  so  far  as  the  formation 
of  available  hydrate  is  concerned.  It  is  fur 
ther  to  be  borne  in  mind  that  the  passivity  of 
the  metal  is  dependent  upon  the  solvent  ac 
tion  of  the  secondary  compounds  as  well  as 
of  initial  ions;  and,  as  presented  beyond,  the 
general  instability  of  aluminum  compounds 
is  very  important  in  this  connection. 


Number  of 
Experiment! 

Averaged. 

Electrolyte. 

Rate  of 

per 

Ampere-Hour. 

Grams 

o  51 

0.77 

O.C)I 

0.57 
0.67 
0.64 

0.58 
0.76 

0.77 
0.58 

0.57 
0.61 

1  8  (1896) 
2 
2 
2 
2 
2 
3 

3 
3 

3 
3 

By  relative 
mentatio 

Filtered  water 

7.84 
II.QO 

9.40 
8.80 
10.30 
9.80 

8.90 
11.70 

11.90 
8.90 

8.80 
9.42 

Carbonic  acid*  

Hydrochloric      and     sulphuric 

Hydrochloric  and   nitric  acids* 
Hydrochloric       and       carbonic 

Hydrochloric,  sulphuric,  nitric, 
and  carbonic  acids*  
Hydrochloric,  sulphuric,  nitric, 
carbonic  acids,*  and  carbonic 

efficiency  in   sedi- 
n   (section   No.  6).  .River  water 

water.     Il   was  Mined   in   several  of  these  experiments  that   dissolved 
aluminum  was  present  in  the  treated  water,  although  its  fcrm  was  nut 
ascertained. 

Rate  and  Form  in  which  Aluminum  leaves  the 
Positive  Pole. 

A.  New  Metal. 

The  rate  at  which  aluminum  leaves  the 
positive  pole  under  the  action  of  an  electric 
current  when  the  electrodes  were  composed 
of  bright  metal  plates  was  determined  at  dif 
ferent  times  and  under  varying  conditions,  as 
shown  in  the  opposite  table. 


B.  In  Practice. 

The  results  in  this  connection,  obtained 
from  long  use  of  the  aluminum  electrodes  on 
a  large  scale,  are  given  in  the  next  table. 

On  account  of  faulty  insulation  of  the  large 
electrodes  no  results  of  positive  value  were 
obtained  with  them  previous  to  May  30. 
From  this  date  to  June  18  one  or  both  of  the 
large  aluminum  electrodes  were  kept  in  prac 
tically  continuous  service.  They  were  re 
moved,  rinsed  and  weighed  nearly  everv  day 
up  to  June  8.  The  deposition  of  the  metal 
and  silt  on  the  negative  pole  caused  the 
weight  of  the  electrodes  to  increase  regularly, 
however,  so  that  these  first  weighings  were  of 
no  value.  On  June  8  electrodes  No.  2  were 
dismantled  and  the  separate  plates  weighed 
and  this  set  rebuilt.  At  this  time  one-half  of 
the  plates  was  left  out  of  the  set,  the  space  be 
tween  plates  doubled,  and  the  direction  of  the 
current  reversed.  The  second  run  from  June 
8  to  12  does  not  therefore  represent  the  ac 
tual  loss  of  metal  of  the  positive  pole,  but  this 
loss  plus  the  loss  in  weight  due  to  the  removal 
of  the  deposited  matter  on  the  surface.  The 
total  ampere-hours  during  this  run  were  58^0 
and  the  loss  of  metal  and  deposit  81  pounds, 
or  at  the  rate  of  6.3  grams  per  ampere-hour. 
Electrodes  No.  4  were  operated  from  June 
3  to  /  and  were  dismantled  and  weighed  on 
June  10.  They  were  operated  again  from 
June  10  to  16,  after  which  frequent  reversals 
of  the  direction  of  the  current  prevented  any 
study  of  the  loss  in  weight  of  any  particular 
portion  of  the  set. 

The    results    of    these    determinations    are 
given  in  the  following  table: 


4o8 


WATER  PURIFICATION  AT  LOUISVILLE. 


SUMMARY    OF    RESULTS. 


Weight  of 


Electrodes    No.    2. 


Electrodes    No.  4-. 


June  12  ) 
"      15  ) 

Total..  . 
Average 

21  470 

20.75 

6.8 

0.44 

66  850 

37.00 

.  .  .  .3.89 

0.25 

In  connection  with  the  above  data  the  fol 
lowing  points  are  to  be  noted: 

1.  The  atomic  weight  of  aluminum  is  27 
and    its   combining   weight    is    generally   ac 
cepted  as  9,  or  in  other  words  its  valency  is  3. 
On  this  basis  the  amount  of  metal  decom 
posed   per  ampere-hour,   assuming   that   the 
full  current  is  active  in  bringing  to  the  anode 
surface    decomposing    ions    to    form    normal 
trivalent  salts,  is  0.34  gram,  or  5.23  grains. 

2.  As  is  generally  known,  certain  salts  of 
aluminum,  notably  those  of  the  mineral  acids, 
are    comparatively    unstable    and    have    the 
power  of  decomposing  the  metal. 

3.  This  supplementary  solvent  action  is  not 
limited  to  the  formation  of  a  basic  salt,  and 
in  fact  may  not  occur  in  this  manner  at  all. 
The    evidence    indicates    that    under    certain 
conditions  which  appear  to  occur  in  electro 
lytic  cells,  the  initially  formed  salt  becomes 
decomposed;    the  metal  separates  out   as  a 
more  or  less  hydrated  oxide;    while  the  acid 
is  free  to  attack  new  metal  and  form  new  salt, 
thus  making  the  action  in  a  measure  con 
tinuous. 

4.  In  an  electrolyte  composed  of  a  com 
bination  of  several  acid  ions  it  is  believed  that 
hydrochloric  acid   attacks   the   metal   to   the 
greatest  extent,  if  not  solely,  and  that  the  re 
sultant  chlorides  are  acted  upon  by  the  other 
acids,  leaving  the  hydrochloric  acid  free  for 
further  solvent  action. 

5.  According     to     Watts,     the     authority 
quoted  in  Chapter  XII,  the  rate  of  decompo 
sition  of  metallic  aluminum  is  0.51  gram,  or 
7.84    grains,    per    ampere-hour.     The    total 
average  results  of  our  experiments  in  August, 
1896,  agree  with  this  very  closely.     If  this 


rate  were  specifically  correct,  and  not  depend 
ent  upon  circumstantial  factors,  it  would  im 
ply  that  the  metal  left  the  electrodes  in  the 
form  of  divalent  salts,  as  in  the  case  of  iron. 

6.  In  view   of  the  fact   that  the  ultimate 
compound  of  aluminum,  the  hydrate,  gives 
every  indication  of  being  in  the  trivalent  form, 
it   would   require   some  atmospheric   oxygen 
dissolved  in  the  water  in  order  to  convert  the 
initial  compounds  into  the  trivalent  hydrate, 
supposing  that  initially   they  were   divalent. 
The  facts  show  that  no  appreciable  diminu 
tion  in  the    dissolved  oxygen  occurred;    and 
this  seems  to  be  substantial  proof  against  the 
divalent  form  of  the  initial  compound,  and  the 
theoretical    rate    of   0.51    gram    per    ampere 
hour,  as  was  indicated  to  be  correct  in  1896. 

7.  With  regard  to  the  formation  of  oxygen 
at  the  anode  the  direct  observations  were  con 
flicting,  but  the  evidence  shows  clearly  that 
even  with  bright  metal  there  is  formed  some 
oxygen  which  attacks  the  metal,  producing 
a   scale   of  alumina   rust    (oxide).     The   rust 
thus  formed,  together  with  a  similar  accumu 
lation  coming  from  the  secondary  reactions 
of  the  initial  salts,  produces  a  surface  coating 
which   not   only   reduces   the   supplementary 
solvent  action,  but  also  gives  to  the  bright 
metal  beneath  the  coating  an  acquired  pas 
sivity. 

8.  In  Chapter  XII  it  is  recorded  that  alu 
minum  hydrate  was  obtained  when  metallic 

.aluminum  was  used  only  for  the  negative  elec 
trodes,  with  the  comment  that  it  was  not  in 
harmony  with  the  present  views  of  electro 
chemistry.  Except  in  a  few  instances  where 
small  amounts  of  aluminum  were  obtained  in 
special  laboratory  experiments,  there  were  no 
indications  from  the  work  in  1897  that  the 
electrolytic  decomposition  of  the  negative 
electrodes  was  a  factor  under  practical  condi 
tions.  However,  it  is  not  unreasonable  to 
suppose  that  under  some  circumstances  the 
strong  alkaline  solution  present  at  the  surface 
of  the  cathode  might  dissolve  this  metal, 
which  has  the  power  of  acting  as  an  acid  and 
of  forming  aluminates. 

In  conclusion  it  may  be  stated  that  the 
available  evidence  taken  as  a  whole  points 
clearly  to  the  decomposition  of  aluminum  un 
der  the  conditions  of  practice  only  at  the  posi 
tive  pole.  Here  it  is  initially  removed  from 


SUMMARY  AND   DJSCUSSION  OF  DATA    OF  1891 


409 


the  plate  as  a  trivalent  salt  of  the  strongest 
acid  ions  ('perhaps  only  in  the  form  of  chlo 
ride).  With  bright  metal  the  plates  are  not 
only  free  from  marked  passivity,  but  the  ini 
tially  formed  salts  appear  to  have  a  supple 
mentary  solvent  action,  with  an  accompany 
ing  deposition  of  rust  upon  the  surface  of  the 
anode.  This  coating,  formed  in  this  manner 
and  by  the  action  of  oxygen,  which  in  small 
quantities  is  set  free  at  the  anode,  gives  event 
ually  to  the  electrode  a  marked  acquired 
passivity  and  reduces  materially  the  supple 
mentary  solvent  action.  In  consequence  of 
this  the  rate  at  which  the  metal  leaves  the 
positive  pole  diminishes  in  time  to  almost  nil, 
although  at  first  a  supplementary  solvent  ac 
tion  causes  it  to  exceed  the  theoretical  by  a 
large,  although  variable,  percentage. 

I'onn  and  Rate  of  Deposition  of  Aluminum  on 
the  Negative  Pole. 

During  the  course  of  the  experiments  by 
the  Water  Company  in  August,  1896,  it  was 
found,  as  has  been  presented  in  Chapter  XII, 
that  aluminum  is  deposited  on  the  negative 
pole  simultaneously  with  the  formation  of  alu 
minum  hydrate.  The  reason  of  this  seems  to 
be  the  same  as  in  the  case  of  iron  electrodes, 
that  a  portion  of  the  metal  from  the  positive 
pole,  which  is  dissolved  by  the  acid  ions,  be 
comes  itself  ionized,  and  acting  as  a  negative 
ion  or  cathion  transfers  a  charge  of  electricity 
from  the  positive  to  the  negative  pole,  where 
on  neutralization  of  the  charge  it  is  deposited 
on  the  face  of  the  plate.  It  is  well  known 
that  electroplating  with  aluminum  is  ex 
tremely  difficult  and  in  some  cases  practically 
impossible,  owing  to  the  rough  and  weakly 
adherent  characteristics  of  the  deposit.  This 
is  just  the  condition  which  was  found  to  exist 
in  the  process  of  formation  of  the  hydrate 
electrolytically,  and  to  the  character  of  the  de 
posit  one  of  the  most  serious  factors  against 
this  process,  aside  from  the  cost  of  the  metal, 
is  due.  It  has  been  found  in  the  course  of 
many  experiments  that  very  finely  divided  silt 
or  clay  particles  suspended  in  the  electrolyte 
are  deposited  upon  the  negative  pole  to  a 
greater  or  less  extent.  This  deposition  of 
silt,  taking  place  at  the  same  time  as  the  depo 
sition  of  the  metal  in  its  porous  form,  results 


in  a  combined  layer  or  deposit  of  silt  and 
metal  of  high  electric  resistance.  The  effect 
of  this  formation  on  the  amount  of  power  re 
quired  is  shown  in  one  of  the  latter  portions 
of  this  section.  The  amount  of  metallic  alu 
minum  contained  in  any  of  the  deposits  found 
in  practice  could  not  be  readily  determined, 
owing,  as  stated  above,  to  the  presence  of  silt. 
Some  idea  of  the  significance  of  this  point  can 
be  obtained  from  the  following  table,  in  which 
the  weights  of  deposits  for  the  several  runs 
with  electrodes  Nos.  2  and  4  are  recorded, 
together  with  the  ampere-hours  of  service 
and  average  rates  of  deposition. 

TABLE    OF    RESULTS. 


Electric 
Period.               Current  in 

AH°r£- 

Weight  of 
Negative 
Electrodes. 

~^~ 

Electrodes  No.  2. 

June3s|           -!53So                 I24 

25.4               I.flJ 

I!     ,*}             583o                    ,4 

24.0               1.56 

Total  51210 

'33 

27.0           1.75 

Electrodes  No.  4. 

JU.?C    36\          .5730 

to 

6.4           0.42 

I!     \l\          *I470 

22 

7-2           0.47 

Total  37200 

32 

6.0           0.39 

Total  for  both 

electrodes..        88410                 170 

13.3          0.88 

Influence  on  flic  I'onnation  of  H\dratc  of  the 
Composition  of  tlic  Rircr  Water. 

The  formation  of  aluminum  hydrate  elec 
trolytically  is  affected  chiefly  by  three  factors: 

1.  Initial  passivity. 

2.  Supplementary  solvent  action  of  the  salt 
formed  when  the  metal  leaves  the  plates. 

3.  Acquired     passivity     due     to     coatings 
formed  on  the  surface  of  the  plates. 

So  far  as  our  observations  went,  no  decisive 
evidence  was  obtained  that  the  composition 
of  the  river  water  materially  affected  the  first 
two  of  these  factors,  but  if  it  did  do  so  the  re 
sult  was  disguised  by  the  third  factor.  The 
formation  of  hydrate  was  influenced  very  ma 
terially  by  the  surface  scales  or  coatings  (caus 
ing  acquired  passivity),  which  are  next  dis 
cussed  with  reference  to  the  composition  of 
the  river  water. 


4io 


WATER   PURIFICATION  AT  LOUISVILLE. 


So  far  as  the  data  go  the  indications  are 
that  the  variations  in  the  character  of  the  river 
water  with  regard  to  dissolved  constituents 
caused  only  a  very  small  percentage  variation 
in  the  amount  of  scale  formation  on  the  posi 
tive  plates.  The  character  and  amount  of  the 
suspended  matter,  however,  exerted  consider 
able  influence  on  the  formation  of  the  deposit 
on  the  negative  plate.  This  is  quite  clearly 
shown  by  the  difference  in  the  increased 
weights  of  electrodes  Nos.  2  and  4,  the  very 
finely  divided  suspended  matter  of  the  last 
days  of  May  greatly  increasing  the  amount  of 
deposit  on  electrodes  No.  2  as  compared  with 
electrodes  Xo.  4,  which  were  operated  some 
what  later.  That  a  certain  percentage  of  this 
fine  material  was  transferred  from  the  positive 
to  the  negative  pole  after  reversing  the  direc 
tion  of  the  current  seems  to  be  the  explana 
tion  of  the  high  rate  of  deposition  with  elec 
trodes  No.  2  from -June  8  to  12.  This  sup 
position  was  borne  out  by  the  change  in  the 
character  of  the  matter  on  the  negative  pole 
after  the  current  was  reversed,  the  presence 
of  the  silt  being  quite  marked  after  the  run 
from  Alay  29  to  June  8,  while  almost  no  silt 
was  found  in  the  scale  after  removal  by  the 
reversed  current.  Some  idea  of  the  signifi 
cance  of  this  action  can  be  obtained  from  the 
following  table,  in  which  the  initial  amount  of 
power  per  ampere-hour  per  gallon  at  the  rate 
of  treatment  of  23.5  cubic  feet  per  minute  is 
given  for  the  start  of  the  first  run  of  each  of 
the  two  sets,  after  15,000  ampere-hours,  and 
for  electrodes  No.  2  at  the  end  of  the  first 
run  (see  "  Form  and  Kate  of  Deposition  on 
Negative  Pole."  page  409). 

HORSE-POWER    REQUIRED    PER    AMPERE-HOUR 
PER   GALLON. 


May  30,  i  i.oo  A.M 
June    i,     =;.oo  I'.M 

"         8,      6.OOA.M 

"       3,     6. oo  r.M 
"       6,    S.OOA.M 


'  The  phites  were  only  rinsed  and  i 


Ampere- 
Hours 
Service 
Since  Last 
Cleaned. 

El-clric 
H.P.  per 
Ampere- 
Hour  per 
Gallon. 

o* 

450 

15  ooo 
45  ooo 

I  2OO 

3080 

o 

240 

15  ooo 

435 

:raped  at  last  cleaning. 

After  the  discussion  of  foregoing  topics  it 
is  obvious  that  the  coatings  or  scales,  com 
posed  of  aluminum  oxide  (rust)  and  clay  par 
ticles,  not  only  increased  the  required  amount 
of  power  very  largely  (shown  above  to  be 
sevenfold),  but  also  increased  the  acquired 
passivity  so  that  with  the  increased  power 
used  there  was  actually  less  aluminum  hy 
drate  produced. 

Influence  on  the  formation  of  Hydrate  of  the 
Presence  of  Scale. 

The  presence  of  coatings  or  scales,  princi 
pally  of  aluminum  rust,  upon  the  surface  of 
the  plates  exerts  a  marked  influence  upon  the 
process,  as  follows: 

1.  It  reduces  the  supplementary  solvent  ac 
tion  of  the  aluminum  salts  and  thus  makes 
the  actual  rate  of  loss  of  metal  at  the  positive 
pole  fall  to  the  normal  rate,  approximately. 

2.  It  gives  to  the  metal  an  acquired  pas 
sivity  which  makes  the  actual  rate  of  hydrate 
formation  drop  far  below  the  normal;   in  fact 
we  have  seen  instances  where  the  formation 
of  hydrate  was  reduced  to  almost  nothing. 

3.  When  the  scale  becomes  very  thick  and 
has  sufficient  tenacity  to  remain  in  place  with 
out  breaking  in   pieces,  we  have   repeatedly 
noted,  especially  for  a  short  time  after  revers 
ing  the  direction  of  the  current,  that  practi 
cally  all  of  the  aluminum  hydrate  remained 
between  the  metal  and  the  layer  of  alumina 
rust. 

4.  From  the  last  table  it  is  plain  that  the 
scale  makes  a  large  increase  in  the  resistance 
to  the  electric  current,  and  the  reduced  rate 
of  formation  is  concomitant  with  an  increased 
amount  of  electric  power. 

Influence  on  the  Process  of  Reversing  the  Direc 
tion  of  the  Electric  Current. 

After  electrodes  have  been  in  service  for 
some  time  the  positive  plates  become  covered 
with  a  scale  of  oxide  and  the  negative  ones 
with  a  more  or  less  heavy  coating  of  deposi 
ted  metal  and  silt.  Under  such  conditions  a 
reversal  of  the  electric  current  results  in  the 
complete  removal  of  the  deposit  from  the  old 
negative  poles  and  the  cessation  of  removal 
of  oxide  scale  from  the  old  positive  poles. 


SUMMARY  AND   DISCUSSION  OF  DATA    OF  1897. 


411 


It  is  difficult  to  determine  in  how  far 
the  reversing  of  the  current  affects  the  rate 
of  formation  of  hydrate.  That  hydrate  was 
formed  in  large  amounts  after  a  reversal  was 
evident  from  inspection,  but,  owing  to  the  fact 
that  the  coating  on  the  old  negative  plates 
retained  a  large  amount  of  the  newly  formed 
hydrate  between  it  and  the  plate,  it  was  not 
possible  to  determine  the  rate  of  formation 
of  the  hydrate.  This  retention  of  the  hydrate 
would  be  a  very  serious  factor  in  practice, 
however,  necessitating  a  mechanical  removal 
of  the  coating  when  the  current  was  reversed. 

In  regard  to  the  effect  of  reversing  the  cur 
rent  on  the  resistance  of  the  electrodes,  the 
evidence  indicates  that  if  a  suitable  means 
could  be  provided  to  remove  the  coating  as 
it  cracks  off  the  old  negative  plates,  a  con 
siderable  increase  in  conductivity  might  be 
gained.  In  practice,  however,  it  is  probable 
that  the  combination  of  the  new  deposit  and 
old  oxide  scale  which  would  form  on  the 
negative  (old  positive)  plates  after  reversal 
would  result  in  increasing  the  resistance  as 
fast  as  or  faster  than  the  removal  of  the  coat 
ing  from  the  positive  (old  negative)  plates 
would  reduce  the  resistance.  Furthermore, 
the  almost  immediate  formation  of  a  layer  of 
hydrate  which  would  be  retained  on  the  new 
positive  poles  would,  unless  removed,  result 
in  an  increase  of  the  resistance.  These  effects 
on  resistance  are  shown  by  the  records  of 
potential  differences  on  cell  Xo.  4  on  July  16, 
17,  and  1 8,  in  the  next  table. 

The  electrodes  were  rinsed  at  6.08  P.M.  on 
July  16  and  the  direction  of  the  electric  cur 
rent  reversed  after  7960  ampere-hours' service 
since  the  plates  were  last  cleaned.  From 
6.30  P.M.  to  12.00  P.M.,  July  16,  the  resistance 
of  the  electrodes  remained  constant  at  0.071 
ohm.  At  12. oo  P.M.  the  direction  of  the  elec 
tric  current  was  reversed.  Tt  was  again  re 
versed  at  6.00  A.M.  and  12.43  P.M.,  July  17, 
and  at  12.30  P.M.,  July  18.  The  records  of 
the  observed  resistance  are  opposite. 

Percentage  of  Metal  U'asfed  in  tliix  Process. 

On  account  of  the  very  irregular  manner 
in  which  the  scale  came  off  from  the  positive 
pole  during  practice,  no  observations  were 
attempted  to  learn  the  relative  percentages  of 


R 

esistanc 

e  in  0 

ims. 

Hour. 

Ju 

y  >7- 

July  ,8. 

A.M. 

• 

.„. 

* 

M. 

12.30 

O.  IO2 

o 

130* 

O 

10           0.124* 

I  .OO 

0.  120 

o 

104 

0 

04           0.088 

I  .30 

O.II6 

o 

'57 

0 

03          0.124 

2.00 

0.  Ill 

o 

168 

0 

04            0.150 

2.30 

0.094 

o 

164 

o 

08           o  .  i  60 

3-00 

0.089 

0 

157 

o 

08           0.162 

3.30 

0.089 

o 

M4 

0 

10            0.162 

4.00 

0.086 

0 

131 

0 

12       i         O.lSj 

4-3" 

0.089 

o 

131 

o 

'3 

5.00 

0.089 

o 

122 

o 

15 

5.30 

0.089 

o 

122 

o 

17 

6.00 

0.089* 

o 

124 

o 

17 

6.30 

0.069 

o 

I'3 

o 

19 

7.00 

0.094 

o 

I'3 

0 

24 

7.30 

0.094 

o 

112 

o 

"3 

8.00 

0.  102 

0 

108 

o 

17 

8.30 

0.089 

o 

104 

o 

17 

9.00 

O.  I  IO 

o 

1  06 

o 

"9 

9-3° 

O.  I  IO 

o 

106 

0 

22 

o  oo 

o.  no 

o 

106 

o 

'9 

0.30 

o.  no 

0 

106 

0 

22 

1.  00 

O.  I  IO 

o 

106 

o 

24 

1.30 

0.  I  10 

0 

106 

o 

24 

2.OO 

0.139 

o 

104 

0 

24 

metal  removed  as  hydrate  and  as  oxide. 
Judging  from  the  results  in  July  and  August, 
1896  (see  Chapters  XI  and  XII),  and  also 
from  observations  of  the  amounts  of  scale  re 
moved  from  the  plates  in  cleaning  during 
1897,  it  is  estimated  that  at  least  50  per  cent, 
of  the  metal  removed  from  the  positive  pole 
was  lost  in  the  form  of  scale,  and  that  from 
i  o  to  20  per  cent,  more  was  deposited  on  the 
negative  plate  in  a  manner  which  made  it 
very  slightly  or  not  at  all  available.  During 
practice  it  would  seem  reasonable  to  figure 
on  an  average  loss  of  about  65  per  cent,  of 
the  metal  removed  from  the  plates. 

Influence  of  Scale  and  Deposit  on  the  Amount  of 
Potvcr  Required. 

This  subject  was  referred  to  under  the  dis 
cussion  of  the  effect  of  the  composition  of  the 
river  water.  As  presented  there  it  was  found 
in  practice  that  the  formation  of  scale  on  the 
positive  poles  and  the  deposit  on  the  nega 
tive  pole  increased  the  amount  of  power  re 
quired  per  ampere-hour  per  gallon  from  240 
electric  II.!'.  with  new  plates  (electrodes 
No.  4)  to  3080  with  old  plates  of  45,000  am 
pere-hours'  service  (electrodes  No.  2).  This 
increase  of  740  per  cent,  does  not  probably 


412 


WATER   PURIFICATION  AT  LOUISVILLE.. 


represent  the  limit  of  the  increase,  as  the  re 
sistances  of  both  electrodes  Nos.  2  and  4 
were  steadily  increasing  at  the  time  they  were 
taken  out  of  service.  Assuming  an  efficiency 
of  50  per  cent,  in  the  formation  of  hydrate  the 
above  figures  represent  an  increase  from  246 
to  1825  electric  H.P.  to  treat  25  million  gal 
lons  per  24  hours  with  the  equivalent  of  i 
grain  per  gallon  of  sulphate  of  alumina. 

The  effect  of  reversal  on  scale  formation 
has  already  been  presented. 

So  far  as  could  be  learned  the  only  possible 
way  to  reduce  the  resistance  of  the  electrodes 
was  to  remove  the  plates  and  scrape  the  sur 
faces  fairly  clean.  This  of  course  involves  a 
considerable  loss  of  metal,  and  its  cost  for  la 
bor  alone  would  make  it  prohibitive.  No 
practicable  means  was  found  of  doing  away 
with  these  scales  and  deposits  with  their  at 
tending  effects. 

Percentage  of  Electric  Power   Wasted   in   this 
Process. 

In  the  formation  of  aluminum  hydrate  by 
this  process  power  is  wasted  in  two  ways: 

1.  A  certain  percentage  of  the  current  is 
transferred  by  ions  which  do  not  attack  the 
pole,  but  decompose  water.     This  current  is 
entirely  wasted  and,  as  power  is  required  to 
produce  it,  such  power  is  lost.     Owing  to  ir 
regularities  in  removal  of  scale  it  was  found 
that  determinations  of  the  amount  of  hydrate 
formed    during    practice    were    not    feasible. 
Basing  the  conclusions  on  the  result  of  many 
laboratory  tests  and  on  the  amount  of  scale 
formed  during  practice,  it  is  estimated  that  not 
more  than  50  per  cent,  of  the  current  is  avail 
able  in  the  formation  of  hydrate,  and  there 
are  indications  that  the  loss  might  at  times 
approach  very  nearly  to  TOO  per  cent. 

2.  The  loss  of  power  due  to  increased  re 
sistance  of  the  electrodes  as  presented  in  pre 
vious  sections  of  this  chapter  reached  as  high 
as  740  per  cent,  of  the  initial  power  required, 
and  the  indications  were  that  the  limit  had 
not  been  reached.     Frequent  scrapings  of  the 
plates,  such  as  would  be  required  to  prevent 
this  increase  of  resistance,  are  impracticable. 

Conclusions. 

With    the   present    knowledge    of   electro 


chemical  actions,  and  with  the  present  cost  of 
aluminum  in  the  form  of  plates  as  contrasted 
with  equal  amounts  of  metal  in  the  form  of 
commercial  sulphate,  the  use  of  hydrate  of 
aluminum  prepared  by  the  electrolytic  decom 
position  of  the  metal  is  out  of  the  question  on 
account  of  cost.  This  is  shown  by  the  fol 
lowing  summary: 

1.  Aluminum  in  sheet  form  costs  in  car 
load   lots   according   to   the  latest   quotation 
27  cents  per  pound.      In  the  form  of  sulphate 
of  alumina  one  pound  of  metal  costs  16  cents. 
The  ratio  of  cost  of  equal  amounts  of  coagu 
lant  prepared  by  the  electrolytical  decompo 
sition  of  the  metal  and  by  the  chemical  de 
composition  of  the  commercial  sulphate  by 
lime  is  therefore  17  to  10  for  aluminum  alone. 

2.  In  operating  there  would  be  a  constant 
loss  of  about  50  per  cent,   of  the  metal  re 
quired  for  the  formation  of  the  hydrate  due 
to  the  passivity  of  the  electrodes  to  the  acid 
ions,  the  supplementary  solvent  action  of  the 
salts  formed,  and  the  consequent  formation 
of  oxide  scale.    This  might  at  times  approach 
100  per  cent. 

3.  The  amount  of  power  required  would 
constantly  increase  with  the  age  of  the  elec 
trodes,  necessitating  at  frequent  intervals  the 
removal  and  scraping  of  the  plates.     This  last 
step  would  be  very  expensive.      Under  nor 
mal  conditions  probably  50  per  cent,  of  the 
normal  power  required  would  be  wasted  in 
overcoming  the  resistance  of  the  surface  coat 
ings.     The  normal  amount  of  power  would 
also  be  increased  from  50  to  100  per  cent,  to 
offset  the  reduced  rate  of  formation  of  hy 
drate,   due  to  the  acquired   passivity  of  the 
metal. 

4.  In  short,  the  process  was  impracticable, 
under  the  conditions  of  these  tests,  both  with 
regard  to  economy  and  regularity  of  produc 
tion  of  hydrate.     While  it  is  probable,  if  not 
certain,   that   prolonged  investigation  would 
improve    the    process    by    using    a    different 
grade  of  metal  and  devising  mechanical  appli 
ances  for  the  removal  of  scales,  yet   in  the 
light  of  our  knowledge,  owing  to  the  inherent 
character  of  the  metal  and  the  narrow  range 
of  conditions  as  applied  to  this  line  of  work, 
commercial  success  of  this  process  seems  to 
be  an  impossibility. 


4'3 


SECTION  No.  6. 

RELATIVE  EFFICIENCY  OF  AVAILABLE  CO 
AGULANTS,  BASED  ON  EQUAL  WEIGHTS 
OF  METAL  USED  AND  ALSO  ON  THE 
AMOUNT  OF  ELECTRIC  CURRENT  IN  THE 
CASE  OF  ELECTROLYTICALLV  FORMED 
COAGULANTS. 

In  order  to  arrive  at  the  most  economical 
coagulant  to  apply  to  the  water,  it  is  essential 
to  know  the  relative  efficiencies  of  those 
available  for  the  purpose.  From  foregoing 
sections  it  is  clear  that  the  available  coagu 
lants  are  four  in  number,  obtained  by  the  fol 
lowing  treatments: 

1.  Sulphate  of  alumina. 

2.  Persulphate  of  iron. 

3.  Electric     current     on     aluminum    elec 
trodes. 

4.  Electric  current  on  iron  electrodes. 

With  the  first  two  (sulphates)  the  compari 
sons  are  expressed  in  their  final  form  with  ref 
erence  to  the  amount  of  metal  contained  in 
the  commercial  products  used  for  the  tests. 
This  is  necessary  because  the  amount  of  metal 
which  determines  the  quantity  of  hydrates 
varies  in  different  lots  of  sulphates  of  the  same 
kind.  The  reason  that  this  is  so  important  is 
that  the  coagulation  is  associated  very  closely 
with  the  volume  of  hydrate  formed.  Further 
more  it  may  be  mentioned  in  passing  that  the 
volume  of  hydrate  formed  depends  upon  the 
specific  gravity  of  the  metal.  Thus  it  has  been 
found  that  one  part  by  weight  of  aluminum 
forms  about  three  times  as  much  hydrate  as 
does  one  part  by  weight  of  iron,  while  the 
specific  gravity  of  iron  is  about  2.8  as  great 
as  that  of  aluminum.  These  general  compari 
sons  will  be  of  much  assistance  in  understand 
ing  the  different  amounts  of  work  done  in  this 
line  by  equal  weights  of  the  two  metals.  A 
record  will  be  found  at  the  foot  of  each  table 
showing  the  amount  of  metal  contained  in 
the  commercial  sulphate  used. 

With  regard  to  the  electrolytic  formation 
of  hydrates  of  these  two  metals,  what  has 
been  said  above  about  volumes  of  hydrate  and 
specific  gravity  of  metals  also  holds  good  in 
this  case. 

Fn  sections  Nos.  4  and  5  it  was  pointed 
out  that  much  of  the  metal  left  the  plate  in 


a  form  non-available  for  coagulation,  and  was 
therefore  wasted.  Practically  it  is  necessary 
under  these  conditions  to  learn  the  amount  of 
electric  current  necessary  to  decompose  and 
convert  enough  available  metal  in  form  of  hy 
drate  to  equal  the  efficiency  of  a  known 
amount  of  metal  in  the  form  of  sulphate. 
With  this  information  in  hand,  and  knowing 
the  total  amount  of  metal  decomposed  and 
removed  from  the  plate,  it  is  possible  to  esti 
mate  how  much  of  the  metal  (and  also  electric 
power)  served  directly  in  producing  coagula 
tion. 

The  evidence  obtained  upon  the  relative 
efficiencies  of  these  coagulants  was  obtained 
in  two  different  ways,  as  follows: 

1.  As  coagulants  in  aiding  subsidence  in 
one-gallon  bottles. 

2.  As   coagulants   in    connection    with    the 
Jewell  filter  and  devices  operated  therewith. 

In  the  first  method  the  percentages  of  re 
moval  of  suspended  matter  were  obtained 
after  24  hours  subsidence.  The  electrolyti- 
cally  formed  hydrates  were  obtained  regularly 
from  bright  metal  electrodes,  and  a  current 
was  applied  for  such  a  period  that  the  theo 
retical  rate  of  decomposition  would  give  an 
amount  of  metal  equal  to  that  in  the  cor 
responding  bottle  in  the  set  with  the  sul 
phates.  In  all  cases  a  series  of  tests  was  made 
with  each  of  the  coagulants  under  considera 
tion,  and  for  a  direct  comparison  of  effi 
ciencies  there  were  selected,  so  far  as  possible, 
those  results  which  came  midway  between  the 
results  of  plain  subsidence  and  complete  clari 
fication.  In  this  manner  the  fairest  compari 
sons  were  made,  and  it  is  these  results  which 
are  given  in  the  tables  beyond. 

Concerning  the  second  portion  of  the  evi 
dence  in  connection  with  the  Jewell  filter,  it 
is  to  be  stated  that,  of  the  185  runs  described 
and  recorded  in  the  first  half  of  this  chapter, 
those  runs  are  selected  which  enable  a  direct 
comparison  to  be  made  of  the  several  coagu 
lants  in  the  purification  of  similar  waters 
under  the  same  general  conditions.  It  is  also 
to  be  borne  in  mind  that  these  conditions  of 
the  second  portion  of  the  evidence  are  those 
of  practice,  and  as  the  electrodes  were  more 
or  less  rusty  the  efficiency  of  the  electric  cur 
rent  was  less  than  on  the  first  set  of  data, 
where  the  tests  were  made  with  bright  metal. 


414 


WATER   PURIFICATION  AT  LOUISVILLE. 


Supplementary  to  these  comparable  data 
were  a  number  of  runs  in  which  the  coagula 
tion  was  insufficient  for  satisfactory  purifica 
tion.  Such  runs  cannot  be  included  in  these 
tables  of  comparable  results,  yet  they  were  of 
much  value  in  showing  and  confirming  the 
range  in  relative  efficiencies  of  the  several  co 
agulants. 


TABLE  SHOWING  THE  RELATIVE  EFFICIENCY 
OF  SULPHATE  OF  ALUMINA*  AND  PERSUL 
PHATE  OF  IRON.f  IN  CONNECTION  WITH  24 
HOURS'  SUBSIDENCE. 


Percentage  Removal. 

Suspended  Solids  in 

Grains  of  Each 

River  Water. 

Chemical  per 

Parts  per  Million. 

Gallon. 

Sulphate  of 

Persulphate  of 

Alumina. 

Iron. 

360                   2.25 

97 

94 

562 

2.50 

93 

97 

I  560 

4.00 

96 

97 

216 

0.75 

80 

So 

553 

1-75 

89 

90 

416 

1-75 

88 

90 

Averages  611 

2.17 

90.5 

9>-3 

*  Containing  9.87  per  cent,  of  aluminum, 
f  Containing  24.  73  per  cent,  of  iron. 

The  above  data  show  that  under  these  con 
ditions  sulphate  of  alumina  and  persulphate  of 
iron,  containing  9.87  and  24.73  Per  cent,  of 
metal  respectively,  possess  substantially  equal 
efficiency,  or  that  the  advantage  lies  very 
slightly  with  the  persulphate  of  iron. 


TABLE  SHOWING  THE  RELATIVE  EFFICIENCY 
OF  PERSULPHATE  OF  IRON*  AND  ELECTRIC 
CURRENT  WITH  IRON  ELECTRODES,  IN  CON 
NECTION  WITH  2J  HOURS'  SUBSIDENCE. 


Suspended 

1'crsulpha 

te  of  Iron. 

Electric 

Current. 

Solids  in  River 

Water. 

Million. 

Gallon. 

Removal. 

Hour  per 
Gallon. 

Removal 

562 

2    50 

93 

0.054 

95 

I  560 

2   00 

91 

0.050 

96 

243 

I    25 

85 

0.031 

87 

216 

I     OO 

90 

0.025 

85 

553 

i   75 

89 

0.045 

88 

272 

2    00 

88 

0.031 

90 

364 

2    OO 

90 

0.037 

91 

Aver.  554 

1.79 

90 

0.039 

90 

*  Containing  24.75  per  cent,  of  iron. 

These  data  show  that  0.039  ampere-hour 
of  electric  current  on  bright  iron  electrodes 


Suspended 
Solids  in  River 

Sulphate  of  Alumina. 

Electric  Current. 

Water. 

C      '                ' 

Ampere-     j 

Parts  per 
Million. 

'Gallon" 

RemSv'af 

Hour  per 
Gallon. 

Percentage 

562 

2.50 

95 

0.023 

94 

I  560 

2.00 

9i 

0.023 

92 

243 

1-25 

85 

0.013 

88 

553 

1-75 

89 

0.015 

90 

416 

1-75 

88 

0.018 

90 

322 

1-75 

88 

o.oiS 

90 

987 

1.50 

94 

0.015 

94 

184 

0.88 

89 

0.015 

88 

[Aver.  603 

1.67 

go 

0.0175 

91 

per  gallon  was  equal  under  these  conditions 
to  1. 79  grains  per  gallon  of  persulphate  of 
iron,  containing  24.73  Per  cent,  of  metallic 
iron.  From  this  it  follows  that  the  amount 
of  iron  decomposed  and  converted  into  the 
form  of  available  ferric  hydrate  per  ampere- 
hour  was  11.3  grains,  which  is  70  per  cent, 
of  the  theoretical  rate. 


TABLE  SHOWING  THE  RELATIVE  EFFICIENCY 
OF  SULPHATE  OF  ALUMINA  *  AND  ELECTRIC- 
CURRENT  WITH  ALUMINUM  ELECTRODES,  IN 
CONNECTION  WITH  24  HOURS'  SUBSIDENCE. 


*Containing  9.87  per  cent,  of  aluminum. 

From  the  above  data  it  is  seen  that  0.0175 
ampere-hour  of  electric  current  on  bright 
aluminum  electrodes  per  gallon  was  equal 
under  these  conditions  to  1.67  grains  per  gal 
lon  of  sulphate  of  aluminum  containing  9.87 
per  cent,  of  metallic  aluminum.  This  shows 
that  there  were  decomposed  and  converted 
into  the  form  of  available  aluminum  hydrate 
9.42  grains  per  ampere-hour.  This  is  181 
per  cent,  of  the  theoretical  rate. 

Comparing  the  efficiency  of  an  electric  cur 
rent  in  the  formation  of  coagulants  by  the  de 
composition  of  bright  metallic  iron  and  bright 
metallic  aluminum,  and  remembering  that  in 
the  last  two  tables  1.67  grains  per  gallon  of 
sulphate  of  aluminum  is  equal  to  1.65  grains 
of  persulphate  of  iron,  it  is  noted  that  0.0175 
ampere-hour  on  aluminum  electrodes  is  equal 
to  0.036  ampere-hour  on  iron  electrodes. 

According  to  these  data  the  electric  current 
is  twice  as  efficient  when  applied  to  aluminum 
electrodes  as  when  applied  to  iron  electrodes. 
From  the  theoretical  rate  of  decomposition 
it  would  be  expected  that  the  relative  effi 
ciency  of  the  current  on  aluminum  and  iron 
electrodes  would  be  0.9  to  i. 


SUMMARY  AND   DISCUSSION  OF  DATA    OF  1807. 


TAHLE  SHOWING 

THE   RELATIVE   EKKICIENCV 

Electric  Current  with  Iron  Electrodes. 

OK     SULPHATE 

OK     AH'N 

IN'A  *     AND     PER- 

SULPHATE   OF    IRON'.f   WHEN    USED    IN   CON 

Suspended 
Number  of         Ampere-      Solids  in  River        Filleted           H-incnal 

NECTION    WITH 

THE   JEWELL    KILTER    AND 

.MiintK.r              Hour  per              Water.      '.        Water.            "j^ 
Ku"                Gallon.             Parts  per         Cubic  Feet       Efficiency. 

ASSOCIATED    DEVICES. 

Million. 

Suspended 

89                  0.040                    330                   15551                98.4 

Number  of 

Grains  per 
Gallon. 

Water. 

Efficiency. 

122              0.097     !            535                  7494            98.4 

Million 

132               0.078                  218          ,       10598             97.5 

147               0.089                 488                   4392             98.3 

148               0.099                 4'9                   5082             97-8 

Sulphate  of  Alui 

nina. 

178               0.040                 128                   7274             98.4 

i 

1.32 

336 

5004 

95-9 

iSl               0.040                  160                   7426             97.5 

8 

1-33 

586 

8540 

99-2 

19 

3-98 

452 

II  986 

95-3 

Averages         0.070                374                 8260            98.2 

347 

97.6 

28 

3.01 

347 

4356 

99.1 

*  Containing  8.46  per  cent,  of  aluminum. 

36 

1.05 

231 

II  296 

99-2 

5° 

1.17 

136 

16  282 

99  .4 

153 

3-33 

352 

7"79 

98.7 

For  the  sake  of  a  more  extended  compari 

Averages 

2.29 

34S 

8898    - 

98.0 

son,  sulphate  of  alumina  is  presented  here  in 

-      Persulphate  of  Iron. 

stead  of  persulphate  of  iron.     From  the  fore 

4 

1.23 

351 

5S59            97-9 

going  table  the  corresponding  amou  it  of  the 

10 

3-99 

586 

1  2  446            99  .  3 

latter  chemical  may  be  substituted  if  desired. 

25 

2.83 

322 

n  304            99.6 

These  data  indicate  that  the  relation  in  ques 

31 

35 

3-37 
1.81 

407 
*93 

8013 

14  556 

99.6 

99-  T 

tion  was  somewhat  variable  but  on  an  average 

51 

1.23 

'3i 

13507 

99.8 

0.070  ampere-hour  of  electric  current  per  gal 

155 

2  .  (>(> 

379 

2617 

99.1 

lon   upon  rustv  iron  electrodes  as  found  in 

Averages 

2.31 

361 

10  560 

99-2 

practice  (with  a  potential  difference  between 

*  Containing  8.46  per  cent. 

of  aluminum. 

plates  of  3  to  5  volts)  was  equal  to  2.25  grains 

f  Containing  24.43  per  c 

:nt.  of  iron. 

per  gallon  of  sulphate  of  alumina  containing 

The  above  comparisons  show  that  persul 

8.46  per  cent,  of  aluminum.   This  corresponds 

phate  of  iron  containing  24.43  per  cent,  of  iron 

to  an  electrolytic  conversion  of  iron  into  the 

is  slightly  hut  distinctly  superior  under  these 

form  of  hydrate  of  9.33  grains  per  ampere- 

conditions   of   sulphate   of  alumina   contain 

hour,  or  58  per  cent,  of  the  theoretical  rate. 

ing  8-4C)  per  cent 

of  aluminum.     This  lot  of 

The  difference  between  this  and  the  70  per 

sulphate  of  alumina  was  not   so  rich  in  alu 

cent,   found  with  bright   iron   electrodes  was 

minum  as  that  used  in  the  subsidence  experi 

due    of    course     o    the    increased     >assivitv 

ments,  and  it  is  fair  to  assume  that  the  relative 

caused  bv  rusting. 

efficiencies    stated     under    those     conditions 

At  this  point  it  may  be  noted  that  in  the 

would  hold  true  in  connection  with  filtration. 

later  comparisons  the  relation  was  found  to 

TABLE    SHOWING 

THE  RELATIVE  EKKICIENCY 

be  in  the  ratio  of  about  o.  10  ampere-hour, 

OK  SULPHATE  OK   ALT  M  INA  *  AND   ELECTRIC 

equivalent  to  2.5  grains  of  sulphate  of  alu 

CURRENT    WITH    IKON     ELECTRODES,  WHEN 

mina,  containing  9.87  per  cent,  of  aluminum 

USED    IN    CONNECTION     WITH     THE   JEWELL 

or  to  the  same  amount  of  persulphate  of  iron 

KILTER  AND    ASSOCIATED 

DEVICES. 

containing  24.73  Per  cent,  of  iron.        From 

careful  inspection  at  the  time  of  the  tests  this 

Suspended 

relation  was  considered  to  be  best  and  was 

Number  of 

Grains  per 
Ga  .    n. 

Solids  in  River 
Water. 

Filtered 

Water. 

Bacterial 
Efficiency. 

so  reported  to  you.     In  view  of  the  fact  that 

Million. 

the  lowest  rate  is  the  safest  one  upon  which 

08 

I     Sf) 

290 

98.0 

to  base  computations,  we  conclude  that  the 

622 

last  comparison  is  the  safest  ratio  under  prac 

125 

3.82 

454 

10381 

99.6 

tical  conditions.     On  this  basis  the  amount  of 

131 
149 

2.70 
2.55 

4"4 

8034 
?6l8 

98.9 
98.0 

iron   decomposed  and  converted   into   avail 

153 
1  80 

3-3" 
0.96 

352 
140 

7679 
10322 

98.7 
97-9 

able  hydrate  would  be  6.17  grains  per  am 

I83 

0.94 

.73 

5457 

96.6 

pere-hour,  or  38  per  cent,  of  the  theoretical 

TAverages 

2.25 

349 

7920 

98.4 

rate  of  decomposition. 

WATER   PURIFICATION  AT  LOUISVILLE. 


TABLE  SHOWING  THE  RELATIVE  EFFICIENCY 
OF  SULPHATE  OF  ALUMINA*  AND  ELECTRIC 
CURRENT  WITH  ALUMINUM  ELECTRODES, 
WHEN  USED  IN  CONNECTION  WITH  THE 
JEWELL  FILTER  AND  ASSOCIATED  DEVICES. 
Sulphate  of  Alumina. 


Snspended 

Number  of 
Run. 

per  Gallon. 

Solids  in 
River  Water. 
Parts  per 

Filtered 
Water. 
Cubic  Feet. 

Bacterial 
Efficiency. 

Million. 

J9 

3.93 

452 

II  986 

95-5 

36 

1.05 

231 

II  296 

99.2 

50 

1.17                    136 

16282 

99-4 

59 

2.47 

301 

6  899 

99-7 

131 

2.70 

288 

8034 

93-9 

Averages 

2.28 

282               10  899 

98.5 

Electric  Current  with  Aluminum  Electrodes. 

Am    ere 

Suspended 
Solids  in 

Filtered 

River  Water. 

Water. 

Run'                Gallon. 

Parts  per 

Cubic  Feet. 

Million. 

20                  0.056 

452 

5  74i 

95-9 

41                   0.020 

242 

5569 

99.0 

49             o.on 

133 

9784 

98.5 

58 

0.028                   453 

3949 

99-5 

133 

0.037 

'59 

6556 

95-2 

Averages 

0.031 

288 

5920 

97.6 

*  Containing  8.46  per  cent,  of  aluminum. 

These  data,  Which  were  obtained  on  the 
whole  under  favorable  conditions,  and  when 
the  plates  were  only  slightly  covered  with 
oxide  coating,  comparatively  speaking,  indi 
cate  that  0.031  ampere-hour  of  electric  cur 
rent  on  aluminum  electrodes  per  gallon  was 
nearly  as  efficient  as  2.28  grains  of  sulphate 
of  alumina  containing  8.46  per  cent,  of  alu 
minum.  One  of  the  disadvantages  of  the 
electric  treatment  which  is  indicated  by  the 
above  data  is  the  diminution  in  the  length  of 
runs  between  washings  and  consequently  in 
the  quantity  of  water  filtered  per  run.  This 
was  due  largely  to  accumulations  of  gas, 
which  retarded  subsidence  under  the  given 
conditions  and  closed  some  of  the  interstices 
of  the  sand  layer. 

Later  experience  with  the  electric  current 
on  aluminum  electrodes  demonstrated  con 
clusively  that  the  above  comparison  was  not 
representative  of  what  would  occur  in  prac 
tice.  After  the  plates  of  the  composition  used 
here  (a  very  pure  commercial  grade)  were 
continued  in  service,  coatings  of  oxide  made 
the  formation  of  hydrate  very  irregular  and 
much  less  than  the  rate  indicated  above. 

Furthermore,   as   was   repeatedly   seen   in 


special  tests,  continuous  service  caused  a  con 
siderable  portion  of  the  aluminum  hydrate  to 
be  non-available,  because  it  became  lodged 
between  the  bright  metal  and  the  surface 
coating. 

Comparing  these  results  with  those  ob 
tained  with  bright  aluminum  electrodes  it  is 
seen  that  t'he  efficiency  dropped  to  about  75 
per  cent,  of  that  recorded  in  the  subsidence 
experiments.  In  view  of  the  fact  that  under 
the  conditions  of  practice  the  percentage  effi 
ciency  steadily  decreased,  the  regular  tests 
with  aluminum  electrodes  were  discontinued 
during  the  latter  portion  of  the  investigations; 
and  the  conclusion  was  drawn  that  unless 
some  practicable  method  of  removing  surface 
coatings  could  be  found,  the  electrolytic 
method  of  forming  aluminum  hydrate  was 
unsafe  and  impracticable,  independent  of  its 
cost,  on  account  of  the  very  low  and  irregu 
lar  formation  of  the  hydrate.  No  practicable 
means  of  removing  the  surface  coatings  on  a 
large  plant  could  be  devised. 


These  comparative  tests  show  that  one 
grain  per  gallon  of  sulphate  of  alumina,  con 
taining  9.87  per  cent,  of  aluminum,  is  equaled 
in  efficiency  as  a  subsiding  and  filtration  co 
agulant  by  one  grain  per  gallon  of  persul 
phate  of  iron,  containing  24.73  Per  cent.  of 
iron,  and  by  0.040  ampere-hour  per  gallon  of 
electric  current  on  iron  electrodes.  With  re 
gard  to  the  action  of  an  electric  current  on 
aluminum  electrodes,  the  process  as  tested 
under  the  most  favorable  conditions  which 
could  be  made  applicable  to  a  large  plant,  was 
found  to  be  unsafe  and  impracticable. 

SECTION  No.  7. 

ECONOMICAL  APPLICATION  OF  COAGULANTS, 
IN  TERMS  OF  SULPHATE  OF  ALUMINA, 
TO  AID  IN  THE  REMOVAL  OF  SUSPENDED 
MATTER  BY  SEDIMENTATION. 

At  the  outset  of  the  consideration  of  this 
portion  of  a  system  of  purification  applicable 
to  the  Ohio  River  water  the  following  facts 
are  to  be  recalled: 

In   the   application   of   coagulants   to   this 


SUMMARY  AND  DISCUSSION   OF  DATA    OF  1897. 


water,  as  it  is  taken  from  the  river,  there  is  a 
great  waste  of  chemicals,  with  an  undesirable 
consequential  effect  upon  the  quality  of  the 
water  from  an  industrial  standpoint;  a  large 
percentage  of  the  normal  filter  plant  would 
have  to  be  duplicated  and  held  in  reserve  for 
use  at  times  of  muddy  water;  the  suspended 
matter  in  the  river  water  varies  so  rapidly  in 
amount  and  character  that  in  the  absence  of 
adequate  subsidence  it  would  be  difficult  to 
manage  a  plant  economically  and  at  the  same 
time  efficiently;  and,  to  correct  these  difficul 
ties,  experience  shows  that  it  is  essential  for 
economical  and  other  reasons  to  remove  as 
much  suspended  matter  as  practicable  from 
the  river  water  by  plain  sedimentation  before 
the  application  of  coagulants. 

I'Yom  what  has  been  said  concerning  plain 
sedimentation  in  section  No.  T  of  this  discus 
sion,  it  will  be  understood  that  during  the 
greater  portion  of  the  year  there  would  be  re 
quired  a  fairly  low  and  approximately  uni 
form  application  of  coagulants  to  the  water 
after  the  removal  of  the  bulk  of  the  suspended 
matter  by  plain  subsidence  and  before  filtra 
tion.  Yet  at  times  (hiring  the  spring  and 
summer  the  amount  of  clay  is  so  great  and 
the  size  of  the  particles  so  small,  that  the  ap 
plication  of  coagulants  can  be  divided  to  ad 
vantage  from  an  economical  point  of  view, 
and  a  portion  of  the  coagulants  employed 
solely  as  an  aid  to  subsidence. 

Many  data  obtained  in  the  course  of  these 
investigations  point  in  this  direction,  but  the 
fact  is  brought  out  most  clearly  by  a  com 
parison  of  the  results  of  runs  Nos.  167  and 
1 68.  which  may  be  briefly  summarized  as  fol 
lows  : 


167 


Grains  pe 

r  Gallon  ol 

Sulphate 

!ji 

£    . 

C 

;  = 

8± 

Jewell 

Settling 
Chamber. 

Total. 

'a  v  " 

£ 

o 

o 
1.49 

2.82 
0.83 

2.82 
2.32 

129 
141 

6556 
15296 

99-3 
99-5 

In  comparing  these  two  runs  it  will  be 
noted  that  the  quality  of  the  river  water  was 
approximately  the  same,  although  the  amount 
of  suspended  matter  was  slightly  higher  in 


the  case  of  No.  168.  With  the  latter  run  the 
total  amount  of  the  divided  application  of  co 
agulants  was  0.5  grain  per  gallon  less  than  in 
the  single  application  in  No.  167.  The  in 
creased  provision  for  subsidence  aided  by  co 
agulation,  about  3  hours  as  compared  with 
0.5  hour,  caused  a  further  removal  of  sus 
pended  matter  as  the  water  reached  the  sand 
layer,  as  shown  by  the  fact  that  the  suspended 
matter  in  the  water  at  the  top  of  the  filter  in 
runs  Xos.  167  and  i(>«X  was  found  to  be  79 
and  15  parts  per  million,  respectively. 

In  consequence  of  this  clearer  but  well  co 
agulated' water  at  the  sand  layer  on  run  No. 
168,  the  quantity  of  water  filtered  between 
washings  was  considerably  more  than  double 
what  it  was  on  run  No.  167,  and  the  percent 
age  of  wash-water  on  Nos.  167  and  168  was 
8.1  and  3.5,  respectively.  In  brief,  with  the 
divided  application  of  chemicals  to  give 
greater  facilities  for  subsidence,  the  amount 
of  coagulants  was  reduced  0.05  grain  per  gal 
lon;  the  quality  of  the  effluent  was  fully  main 
tained;  and  the  capacity  of  the  filter  was 
materially  increased. 

With  i .06  grains  per  gallon  of  sulphate  of 
alumina  applied  at  basin  No.  I  and  i.io  to 
1.13  grains  at  the  Jewell  settling  chamber, 
there  was  a  slight  loss  in  economy  with  the 
divided  application,  in  purifying  a  water  con 
taining  rather  more  suspended  matter  than 
in  the  case  of  runs  Nos.  167  and  168,  as 
shown  by  runs  Nos.  163  and  164. 

The  use  of  0.65  grain  per  gallon  of  sul 
phate  of  alumina  at  basin  No.  i,  in  addition 
to  i. 20  grains  at  the  Jewell  settling  chamber, 
was  found  to  be  inadequate  for  the  purifica 
tion  of  this  water,  as  shown  by  runs  157  and 
158. 

The  practical  conclusions  to  be  drawn  from 
this  experience  are  that  with  preliminary  co 
agulation,  followed  by  subsidence  for  a  period 
of  about  3  hours,  the  application  of  coagu 
lants  may  be  divided  to  advantage,  and  a  con 
siderable  portion  of  the  suspended  matter 
kept  off  the  filter,  when  the  total  amount  of 
required  coagulant  ranges  from  2  to  2.5 
grains  or  more  of  ordinary  sulphate  of  alu 
mina  per  gallon.  In  the  case  of  a  water  re 
quiring  more  than  this  amount  of  coagulating 
treatment,  a  proper  division  of  the  application 
would  increase  the  saving  of  coagulants  and 


4i8 


WATER   PURIFICATION   AT  LOUISVILLE. 


would  diminish  the  frequency  of  washing  the 
filter. 

To  place  an  estimate  upon  the  minimum 
limit  of  suspended  matter  in  the  water  where 
a  division  in  the  application  could  be  profit 
ably  made  is  difficult,  owing  to  the  wide 
range  in  the  character  of  the  suspended  mat 
ter;  and.  further,  the  period  of  subsidence  fol 
lowing  the  preliminary  application  of  coagu 
lants  is  an  important  factor  and  was  too  short 
in  these  devices.  Under  the  existing  condi 
tions  it  was  found  necessary  to  apply  about 
1.5  grains  per  gallon  of  sulphate  of  alumina 
in  order  to  make  preliminary  coagulation  and 
subsidence  effective.  With  a  longer  period 
of  subsidence  this  quantity  could  possibly  be 
lessened  somewhat.  But  before  consider 
ing  further  the  practical  significance  of  these 
facts  we  will  show  why  it  is  necessary  to  apply 
a  certain  considerable  amount  of  coagulating 
chemicals  in  order  that  coagulation  and  sub 
sidence  may  be  efficient. 

Relative  Efficiencies  in  Sedimentation  of  Differ 
ent  Amounts  of  Coagulants. 

in  studying  the  behavior  of  coagulants  in 
connection  with  the  sedimentation  and  filtra 
tion  of  the  Ohio  River  water,  the  most  notice 
able  feature  is  that  in  the  case  of  sulphate  of 
alumina  very  little  appears  to  be  accom 
plished  until  the  quantity  of  applied  chemical 
reaches  a  certain  amount,  ranging  with  differ 
ent  waters  from  0.75  to  1.50  grains  per  gal 
lon. 

The  indications  are  that,  before  any  practi 
cal  coagulation  is  effected,  a  certain  amount 
of  coagulant  must  be  applied  in  order  that  the 
absorptive  and  perhaps  other  similar  capaci 
ties  of  the  suspended  matter  in  the  water  be 
completely  satisfied.  In  connection  with  the 
explanation  of  this,  reference  is  made  to  the 
close  of  section  No.  2  of  this  discussion. 

Persulphate  of  iron  and  electrolytically 
formed  hydrates  of  iron  and  aluminum  behave 
in  a  similar  manner  to  sulphate  of  alumina,  as 
shown  by  the  results  of  experiments  recorded 
in  the  next  set  of  tables. 

These  results  are  representative  of  many 
data  obtained  in  the  laboratory,  where  sub 
sidence  for  24  hours  after  the  application  of 
the  coagulant  took  place  in  one-gallon  bot 
tles. 


Attention  is  especially  called  to  the  last  col 
umn,  where  the  increase  in  the  removal  of 
suspended  matter  for  successive  portions  of 

the  coagulant  is  shown. 

Sulphate  of  Alumina. 

(River  water  contained  424  parts  per  million  of  suspended 
matter.) 


After  Settli 

,g24  Hours 

Applied 

Additional 

per  Gallon. 

Solids. 
Parts 
per  Million. 

Percenta.ee 
Removal. 

for  Successive 
Portions 
of  0.25  Grain. 

N 

0.25 
0.50 
0.75 

I.OO 

1.25 
1.50 

47 
44 

35 
3 

o 

74 

76 

97 
99 
too 

4 
2 
5 
1  6 

T 

Persulphate  of  Iron. 

(River  water  contained  364  parts  per  million  of  suspended 
matter.) 


After  Settli 

g  24  Hours. 

Additional 

A  pplied 
Chemical.    Grains 
per  Gallon. 

Suspended 
Solids. 

Percentage 

Removal 



Parts 
per  Million. 

Removal. 
65 

0.40 
o.So 

122 

123 

66 
66 

I 
O 

1.20 

120 

67 

I 

1.  6() 

67 

82 

15 

2.OO 

38 

90 

8 

2.40 

28 

92 

2 

2.  SO 

7 

98 

6 

3.20 

2 

99 

I 

Electric  Current  with  Iron  Electrodes. 

(River  water  contained  424  parts  per  million  of  suspended 
solids.) 


After  Settlin 

;  -24  Hours. 

Additional 

Treatment. 
Ampere-Hour 

Suspended 

Removal  for 
Successive 

per  Gallon. 

Parts  per 
Million. 

Removal. 

Ampere-  Hour. 

None 

185 

cfi 

O.OI2 

I  So 

58 

2 

o.oiS 

167 

6  1 

5 

0.025 

161 

62 

i 

o  .  03  1 

156 

63 

I 

0.038 

'44 

66 

3 

0.044 

123 

71 

5 

0.062 

26 

94 

23 

0.096 

5 

98 

4 

o  124 

o 

IOO 

2 

SUMMARY  AND   DISCUSSION   OF  DATA    OF  1897. 


419 


Electric  Current  ivith  Aluminum  Electrodes. 

(River  water  contained  364  parts  per  million  of  suspended 
solids.) 


After  Settlin 

J  24  Hours. 

Additional 

Removal  for 

Suspended 

Reemonvaf 

Million. 

Ampere-  Kour. 

None 

67 

O.OO2 

96 

74 

7 

0.005 

«7 

76 

2 

0.008 

82 

77 

I 

0.010 

So 

78 

I 

0.013 

44 

88 

IO 

0.015 

34 

91 

3 

0.018 

20 

94 

3 

O.O2O 

JO 

97 

3 

0.023 

3 

99 

" 

The  above  results  show  that  with  these 
waters  it  was  necessary  to  apply  from  i.o  to 
1.6  grains  of  sulphate  of  alumina  per  gallon 
before  subsidence  caused  a  material  removal 
of  suspended  matter,  in  addition  to  that  re 
moved  by  plain  subsidence.  It  is  true  that 
these  waters  contained  more  silt  than  ought 
ordinarily  to  be  the  case  in  practice  after  plain 
subsidence  had  taken  place.  With  suspended 
matter  of  a  clayey  nature  this  minimum 
amount  of  coagulant  for  efficient  coagulation 
would  probably  be  reduced. 

Just  how  far  the  conditions  of  practice 
would  cause  the  minimum  efficient  amount 
of  coagulant  to  depart  from  that  indicated 
above  was  impracticable  to  ascertain  ac 
curately  under  the  conditions  of  these  inves 
tigations. 

There  are  indications  that  the  minimum 
limit,  where  the  division  in  the  application  of 
coagulant  would  be  economical,  would  fall 
below  2  grains  of  ordinary  sulphate  of  alu 
mina  and  perhaps  as  low  as  1.5  grains  per 
gallon.  As  it  requires  about  0.75  grain  as  a 
minimum  application  to  secure  coagulation 
prior  to  filtration,  this  would  leave  an  equal 
quantity  of  coagulant  to  facilitate  subsidence. 

SECTION  No.  8. 

EFFECT  OF  THE  PERIOD  OF  COAGULATION  OF 

THE  OHIO  RIVER  WATER  BEFORE 

FILTRATION. 

Recently  there  have  developed  in  some  lo 
calities  differences  in  opinion  as  to  the  most 


advantageous  period  of  time  to  intervene  be 
tween  the  application  of  the  coagulant  and 
the  entrance  of  the  water  into  the  sand  layer. 
The.  data  bearing  on  this  point  are  presented 
in  the  next  two  tables,  and  the  conditions  un 
der  which  they  were  obtained  are  outlined  as 
follows: 

Table  No.   i. 

In  this  table  a  comparison  is  made  of  the 
principal  data  in  13  pairs  of  runs  showing  the 
efficiency  of  the  Jewell  filter  when  the  coagu 
lant  (sulphate  of  alumina)  was  applied  at  the 
inlet  and  outlet  of  the  settling  chamber,  re 
spectively.  It  will  be  recalled  that  the  outlet 
of  the  settling  chamber  was  at  the  top  of  the 
filter.  When  the  coagulant  was  applied  at 
the  inlet  to  the  settling  chamber  the  period  of 
coagulation  averaged  about  30  minutes,  and 
when  applied  to  the  mouth  of  the  pipe  lead 
ing  from  the  settling  chamber  to  the  upper 
compartment  (containing  about  1.6  feet  of 
water)  above  the  sand  layer,  the  period  was 
about  8  minutes.  The  character  of  the  Ohio 
River  water  was  such  during  these  runs  that 
the  average  quantity  of  coagulant  was  ap 
proximately  equal  to  the  estimated  annual 
average  amount  required  for  the  water  under 
favorable  conditions  for  purification. 

Table  No.  2. 

A  comparison  of  the  principal  data  of  runs 
Xos.  173,  174,  and  175  with  the  Jewell  filter 
is  made  in  this  table. 

At  this  time  the  river  water  contained 
much  less  suspended  matter  than  on  the  runs 
recorded  in  Table  No.  I.  The  coagulant  on 
these  three  runs  was  applied  at  the  inlet  to 
basin  Xo.  i,  the  inlet  to  the  Jewell  settling 
chamber,  and  to  the  outlet  of  the  latter  cham 
ber,  respectively.  This  made  the  average 
periods  for  coagulation  about  199,  30,  and  <S 
minutes,  respectively. 

Comparing  the  average  results  of  Table 
No.  i,  it  is  seen  that  with  the  same  character 
of  river  water  the  change  in  the  point  of  ap 
plication  of  the  coagulant  from  the  inlet  to 
the  outlet  of  the  settling  chamber  (reducing 
the  period  of  coagulation  from  30  to  8  min 
utes)  caused  the  quantity  of  water  filtered 


420 


WATER    PURIFICATION  AT  LOUISVILLE. 


TABLE    No.   1. 

COMPARISON  OF  THE  EFFICIENCY  OF  THE 
JEWELL  FILTER  WHEN  THE  COAGULANT 
WAS  APPLIED  AT  THE  INLET  TO  THE 
SETTLING  CHAMBER,  AND  WHEN  IT  WAS 
APPLIED  TO  THE  WATER  AT  THE  TOP 
OF  THE  FILTER. 

Coagulant  Applied  at  the  Inlet  to  the  Settling 
Chamber. 


Number 
of 
Run. 

Suspended 
Solids  in 
River  Water. 
Parts  per 
Million. 

Applied 
Sulphate  of 
Alumina. 
Grains  per 
Gallon. 

Filtered 
Water. 

Cubic  Feet. 

Bacterial 
Efficiency. 

94 

149                     2.H 

17  898 

97-9 

97 

300                     1.33 

2  IO5 

95.6 

98 

296                     1  .  46 

5942 

98.0 

IO2 

368                      1.69 

4  609 

96.7 

104 

438                    i.  88 

8367 

98.8 

140 

124                    1.67 

26  640 

98.2 

143 

548 

1-52 

(>  137 

97-9 

145 

438 

1.92 

II  584 

99.2 

I64 

189 

I.8l 

4  200 

98.9 

1  66 

189 

2.14 

4  218 

99  •" 

176 

130 

I.  O2 

18435 

98.0 

1  80 

140 

0.78 

TO  322 

97-9 

183 

173 

0.77 

5457 

96  .  6 

Averages 

268 

1-55 

9  686 

97.8 

Coagulant  Applied  at  the  Top  of  the 

Filter. 

92 

2IO 

2-47 

44f>3 

98.1 

93 

140 

1.92 

5  5f>7 

97-9 

95 

184 

2-74 

I  013 

98.7 

96 

3OO 

i-3i 

I  048 

96.7 

99 

295 

1.42 

55iS 

95-7 

101 

350 

1.87 

999 

97-5 

103 

368 

i  .92 

2856 

98.1 

141 

552 

1-59 

I  300 

97-7 

142 

548 

2.02 

4  210 

98.9 

i65 

189 

2.  IO 

I  187 

97  .  8 

175 

130 

I.  60 

10  565 

99-2 

179 

127 

1.04 

I  007 

97.0 

184 

174 

I  .  IO 

I  071 

97-0 

Averages 

274 

1.78 

3139 

97-7 

TABLE  No.  2. 

COMPARISON  OF  THE  EFFICIENCY  OF  THE 
JEWELL  FILTER  WHEN  THE  COAGULANT 
WAS  APPLIED  AT  THE  INLET  TO  HASIN 
NO.  1,  THE  INLET  TO  THE  JEWELL  SET 
TLING  CHAMBER  AND  THE  OUTLET  OF 
THE  LATTER  (TOP  OF  FILTER),  RESPECT 
IVELY. 


Application  of  Sulpha 

teof 

»±i 

Alumina. 

^.*s 

Sj  . 

J 

g 

Place. 

ex  c 

||| 

•o  u 

«! 

3 

SO 

2  c  C-. 

—  U 

rt  ^ 

7, 

O 

X 

fc 

B3 

173 

Inlet,  Basin  No.   I.. 

I-5I 

74 

32  227 

99.0 

174 

j  Inlet    Jewell    Set- 
(  tling  Chamber.  ... 

I.  60 

73 

20438 

99.0 

T  TCI 

between  washings  to  be  diminished  to  about 
one-third;  and  this  reduction  was  accom 
plished  when  the  quantity  of  coagulant  was 
increased  15  per  cent. 

The  character  of  the  filtered  water  was 
unchanged,  except  perhaps  it  should  be 
noted  in  this  connection  that  it  was  a 
failure  in  the  quality  of  the  effluent  which 
caused  the  filter  to  be  washed  in  all  runs  re 
corded  in  Table  No.  i,  excepting  No.  140,  on 
which  run  the  rate  failed  with  a  satisfactory 
effluent. 

This  means  that  with  the  shorter  period  of 
coagulation  the  quality  of  the  effluent  failed 
more  quickly  than  in  the  case  of  the  regular 
period.  In  this  connection  it  is  to  be  pointed 
out  that,  while  the  amount  of  the  suspended 
matter  in  the  river  water  was  the  same  in  each 
case,  the  suspended  matter  in  the  water  as  col 
lected  from  above  the  sand  layer  averaged  90 
and  1 60  parts  per  million  with  the  long  and 
short  periods,  respectively. 

With  regard  to  the  data  in  Table  No.  2  the 
river  water  contained  less  suspended  -matter 
than  in  the  case  of  the  water  dealt  with  in 
the  first  table,  and  the  amount  of  coagulant 
was  relatively  greater,  with  a  consequently 
higher  bacterial  efficiency. 

Under  these  conditions  the  ratio  of  the 
quantities  of  filtered  water  per  run,  when  the 
coagulant  was  applied  at  the  inlet  and  the  out 
let  of  the  settling  chamber  was  2  to  i  instead 
of  3  to  i,  as  in  the  case  cited  above.  In  a  gen 
eral  way  this  diminution  in  the  effect  of  the 
period  of  coagulation  was  repeatedly  ob 
served  as  the  water  became  clearer. 

On  runs  Nos.  173,  174,  and  175  the  sus 
pended  matter  in  the  water  on  the  top  of  the 
filter  was  found  to  be  21,  45,  and  86  parts  per 
million,  respectively.  As  would  naturally  be 
expected,  the  longest  and  most  satisfactory 
run  was  the  one  on  which  the  amount  of  sus 
pended  matter  going  on  the  filter  was  the 
least.  All  things  considered,  this  run,  No.  173, 
on  which  the  period  of  coagulation  was  about 
3.3  hours,  was  the  most  satisfactory  one  ob 
tained  during  the  entire  series  of  experiments. 
It  brought  out  very  clearly  the  fact  that  the 
period  of  coagulation  could  with  marked  ad 
vantage  be  made  much  longer  than  custom 
formerly  supposed. 

It  is  not  to  be  inferred  that  in  all  cases  a 


SUMMARY  AND   DISCUSSION  OF  DATA    OF  1897. 


period  of  3.3  hours  for  coagulation  is  desir 
able  or  even  admissible  from  a  practical 
standpoint. 

The  facts  as  illustrated  by  runs  Nos.  182 
and  183  show  that  this  is  not  true.  With 
about  0.75  grain  per  gallon  of  sulphate  of  alu 
mina  applied  to  river  Water  containing  172 
parts  per  million  of  suspended  matter,  at  the 
inlet  to  basin  No.  i  and  the  Jewell  settling 
chamber,  respectively,  the  application  at  the 
first  point  resulted  in  the  run  being  a  failure, 
while  in  the  second  case  fair  results  were  ob 
tained. 

As  stated  in  section  No.  i,  the  decom 
position  of  commercial  sulphates  in  moderate 
amounts  by  the  alkaline  constituents  of  the 
Ohio  River  water  is  practically  instantaneous. 
Butthe  amount  and  character  of  the  suspended 
matter  in  the  water  exert  considerable  in 
fluence  upon  the  optimum  period  of  coagula 
tion  for  a  given  water.  This  is  shown  by 
inspection  of  the  data,  when  it  will  be  noted 
that  different  amounts  of  coagulants  were  re 
quired  to  yield  satisfactory  results  from 
waters  apparently  similar,  so  far  as  could  be 
told  from  amounts  of  suspended  matter.  In 
general  terms  these  last  observations  hold 
true,  practically  speaking,  for  electrolytically 
formed  coagulants. 

Conclusions. 

1.  The  Ohio  River  water  as  it  comes  from 
the  river,  and  also  after  the  coarse  matters  are 
removed  from  it  by  plain  subsidence,  requires, 
for  its  most  economical  and  efficient  treat 
ment,  different  periods  of  coagulation  at  dif 
ferent  times,  according  to  the  character  and 
amount  of  suspended  matter. 

2.  When   the   water  is  very   clear  the  in 
dications  are  that  but  little  difference  would 
be  noted  in  periods  of  from  i  to  30  minutes; 
and,   further,   with   clear  water  it   is   proba 
ble    that    if   the    period    were    extended    be 
yond  this  range  to  a  certain  but  not  well- 
defined  point,  a  loss  in  efficiency  would  result. 

3.  But  when  the  water  contains  its  usual 
amount  and  character  of  suspended  matter 
the  period  of  coagulation  to  give  the  best  re 
sults  is  a  variable  one,  and  reaches  several 
hours  in  length  before  a  division  in  the  appli 


cation  of  coagulants  (as  discussed  in  section 
No.  7)  becomes  advisable. 

4.  To  fix  upon  any  given  period  to  give 
uniformly,  under  the  conditions  of  success 
ful  practice,  the  optimum  degree  of  coagula 
tion,  or  very  nearly  so,  does  not  seem  prac 
ticable  in  the  light  of  our  present  knowledge; 
and  it  is  recommended  that  for  a  large  plant 
the  devices  for  .the  application  of  coagulants 
be  made  adjustable,  so  as  to  vary  the  period 
of  coagulation  as  the  character  of  the  water 
demands.     Whether  or  not  it  would  ever  be 
advisable  to  fix  the  point  of  application,  so 
as  to  give  a  constant  period  of  coagulation, 
can  only  be  told  by  practical  experience. 

5.  With  regard  to  the  best  period  of  coagu 
lation  for  subsidence,  when  a  division  is  made 
in  the  application  of  coagulants,  it  must  be 
borne  in   mind  that  under  these  conditions 
two  objects  are  sought,  the  coagulation  of  the 
suspended  articles  and  their  removal  by  sedi 
mentation.     While  it  is  probable  that  sedi 
mentation  might  take  place  more  rapidly  if 
the   coagulation    was    completed    before    the 
suspended    matters   began    to    subside,    than 
when  these  two  actions  took  place  simultane 
ously,  experience  indicates  quite  clearly  that 
a  saving  is  made  by  allowing  sedimentation 
to  take  place  during  coagulation.   The  period 
of  coagulation,  being  plainly  the  shorter,  be 
comes  therefore  unimportant,  as  the  optimum 
period  of  subsidence  with  coagulation  would 
be  the  controlling  factor. 

The  conditions  of  these  investigations  were 
not  such  as  to  allow  the  study  of  the  optimum 
period  of  subsidence  with  coagulation,  of  a 
water  which  had  already  been  partially  puri 
fied  by  plain  subsidence.  It  may  be  stated, 
however,  that  as  the  water  after  proper  pre 
liminary  treatment  by  plain  subsidence  would 
contain  only  relatively  fine  suspended  parti 
cles,  the  optimum  period  would  probably  be 
considerably  longer  than  would  be  indicated 
by  the  results  of  subsidence  with  coagulation 
of  a  water  which  had  not  been  properly  set 
tled.  Experiments  on  the  direct  treatment  of 
river  water  such  as  were  recorded  in  Chapter 
IV,  and  in  previous  sections  of  this  chapter, 
do  not  therefore  apply  to  the  subject  in  hand 
except  in  a  very  general  way. 


422 


WATER  PURIFICATION  AT  LOUISVILLE. 


SECTION  No.  9. 

DEGREE  OF  COAGULATION  OF  THE  WATER 
BEFORE  FILTRATION, AND  THE  MINIMUM 
AMOUNT  OF  COAGULANT  REQUIRED  FOR 
THAT  PURPOSE. 

In  all  cases  experience  showed  that  for  suc 
cessful  filtration  the  coagulation  of  the  water 
as  it  enters  the  sand  layer  must  be  practically 
complete.  To  a  trained  operator  of  a  filter 
this  condition  of  the  water  can  be  noted  quite 
accurately  by  inspection.  It  can  be  described 
by  the  statement  that  the  suspended  matters 
in  the  water  must  have  a  "  curdled "  or 
"  flakey  "  appearance,  which  is  such  that  ulti 
mately  the  suspended  matters  would  subside 
and  leave  the  water  in  a  practically  clear  con 
dition.  The  rate  at  which  such  subsidence 
would  take  place  depends  largely  upon  the 
size  and  specific  gravity  of  the  matters  in 
suspension. 

It  was  found  that  the  proper  degree  of  co 
agulation  of  this  water  as  it  entered  the  sand 
layer  was  the  sine  qua  non  of  economical  and 
efficient  purification  by  the  American  type  of 
filters.  From  what  is  said  in  the  paragraph 
above  it  is  not  to  be  inferred  that  subsidence 
alone  is  adequate  under  practicable  condi 
tions  for  satisfactory  purification.  It  is  essen 
tial  to  have  filtration  in  order  to  make  the 
purification  complete.  The  amount  of  sus 
pended  matter  in  the  water  affects  the  degree 
of  coagulation  only  in  that  the  amount  of  co 
agulant  must  be  sufficient  to  yield  enough 
gelatinous  hydrate  to  envelop  practically  all 
of  the  suspended  particles,  including  the  bac 
teria. 

Coagulation  of  the  water  entering  the  sand 
need  not  if  necessity  be  absolutely  complete 
so  far  as  maximum  formation  of  size  of  flakes 
is  concerned,  because  the  friction  in  the  sand 
layer  will  supplement  this  action  if  the  volume 
of  hydrate  is  sufficient.  This  is  especially  true 
of  the  middle  and  latter  portions  of  runs, 
when  considerable  hydrate  is  accumulated  in 
and  upon  the  sand  layer.  Concerning  a  volume 
of  hydrate  in  excess  of  that  capable  of  giving 
the  above  conditions,  it  is  to  be  avoided  not 
only  because  it  is  a  waste  of  chemicals  (and 
unnecessarily  increases  the  corroding  and  in- 
crusting  constituents  of  the  effluent  in  the 
case  of  sulphates),  but  because  it  increases 
the  frequency  of  washing  the  sand  layer  and 


consequently  reduces  the  capacity  of  the  fil 
ter. 

In  view  of  the  fact  that  during  the  greater 
portion  of  the  year  the  Ohio  River  \vater  con 
tains  clay  particles  which  are  smaller  than 
bacteria,  the  bacterial  efficiency  is  generally 
satisfactory  if  the  filtered  water  is  clear  and 
free  from  turbidity.  As  a  matter  of  fact,  in 
many  cases  during  the  tests  recorded  in  this 
chapter  very  fair  bacterial  efficiency  was  ob 
tained  when  the  effluent  was  so  turbid  that 
the  run  was  stopped,  the  filter  washed,  and 
the  amount  of  coagulant  increased  for  the 
next  run.  However,  there  are  also  times  dur 
ing  the  winter  when  the  suspended  matter  is 
so  coarse  that  comparatively  little  difficulty 
is  experienced  in  getting  a  bright  or  even 
brilliant  effluent,  while  a  satisfactory  removal 
of  bacteria  was  a  less  easy  matter 

This  consideration  of  the  relative  difficulty 
in  removing  bacteria  and  finely  divided  clay 
brings  us  to  the  question  of  the  minimum 
amount  of  coagulant  which  can  properly  be 
applied  to  this  water.  Experience  indicates 
that  under  ordinary  circumstances  this  river 
water  would  rarely  if  ever  reach  a  condition 
where  less  than  0.75  grain  per  gallon  of  sul 
phate  of  alumina,  containing  about  9.87  per 
cent,  of  aluminum,  could  be  used  with  safety 
in  this  method  of  purification. 

SECTION  No.   10. 

ON    THE    CONDITIONS    OF    SUCCESSFUL 
FILTRATION. 

In  addition  to  a  confirmation  of  the  evi 
dence  in  Chapter  IX,  our  knowledge  upon 
the  conditions  of  successful  filtration  was  ad 
vanced  in  several  particulars.  But  as  it  was 
considered  feasible  to  operate  only  one  filter 
during  the  tests  described  in  this  chapter, 
comparative  data  are  scant}-  or  lacking  along- 
several  lines,  notably  those  related  to  the 
character  of  the  sand  layer,  such  as  thickness 
and  size  of  grain.  The  principal  information 
of  practical  value  obtained  in  this  connection 
during  1897  is  as  follows: 

Amount   of   Suspended   Matter   in   the    Water 

Reaching  tJie  Sand  Layer,  and  the 

.  Coagulation  of  the  Same. 

Experience  during  the  last  portion  of  the 
tests  (April  to  July,  1897)  demonstrated  con- 


SUMMARY  AND   DISCUSSION   OF  DATA    OF  ISO", 


423 


clusively  that  for  the  uniform,  efficient,  and 
economical  filtration  of  the  Ohio  River  water 
it  is  imperative  to  remove  the  suspended  mat 
ter  so  far  as  practicable  from  the  water  before 
it  reaches  the  sand  layer.  The  data  confirm 
in  a  decisive  manner  the  conclusion  drawn  in 
1896,  that  filtration  alone  is  inadequate  for 
the  successful  purification  of  the  silt  and  clay- 
bearing'  Ohio  River  water.  Filtration  is  the 
last  step,  and  a  very  important  and  essential 
one,  in  a  method  in  which  sedimentation, 
plain  and  with  coagulation,  precedes  filtra 
tion. 

By  plain  subsidence,  supplemented  at  times 
by  subsidence  with  coagulation,  there  arc 
gained  a  number  of  distinct  advantages,  as 
were  pointed  out  before,  as  follows: 

i.  A  considerable  wastage  of  coagulants 
would  be  prevented — an  amount  much  ex 
ceeding  the  cost  of  subsidence. 

j.  The  cost  of  construction  and  main 
tenance  of  a  large  reserve  portion  of  a  plant, 
to  aid  in  handling  muddy  water,  would  be 
obviated. 

3.  The   efficiency    of   the    plant    would   be 
more  uniform  and  satisfactory  with  regard  to 
the  quality  of  the  effluent. 

4.  The  difficulties  and  cost  of  operating  a 
plant  to  purify  with  uniform  satisfaction  the 
very  variable  Ohio  River  water  would  be  re 
duced  largely.     In  this  connection  reference 
is  especially  made  to  the  adjustment  of  the 
optimum   amount   of   coagulant    and    to   the 
cleansing  of  the  sand  layer. 

At  this  point  the  very  important  question 
arises,  What  amount  of  suspended  matter  can 
be  properly  handled  by  filters  of  the  American 
type  ? 

Much  thought  has  been  directed  to  an  ex 
pression  of  this  amount  by  weight  in  parts 
per  million.  \Ve  have  not  succeeded,  how 
ever,  in  fixing  the  limit  in  this  manner,  ow 
ing  to  the  wide  discrepancies  obtained  in 
handling  equal  weights  of  suspended  matter 
of  different  character.  Thus  at  times  100 
parts  per  million  of  fine  clay  were  more  diffi 
cult  to  remove  than  500  parts  of  silt. 

The  best  way  in  which  we  can  express  this 
amount  is  by  the  statement  that  by  plain  sub 
sidence,  aided  by  coagulation  when  necessary, 
the  suspended  matter  in  this  river  water 


should  be  reduced  to  a  point  where,  by  filtra 
tion  and  the  coagulation  just  preceding  it, 
the  remaining  suspended  matter  can  be  re 
moved  by  the  final  application  of  coagulants 
not  exceeding  1.5  to  2  grains  per  gallon  of 
ordinan-  sulphate  of  alumina,  or  its  equiva 
lent. 

In  section  Xo.  9  it  was  stated  that  for  suc 
cessful  filtration  the  final  application  of  co 
agulants  must  be  such  that  the  coagulation  of 
the  suspended  particles  is  practically  com 
plete.  When  the  coagulation  is  complete,  it 
follows,  as  shown  by  experience,  that  the 
period  of  coagulation  may  be  extended  so  as 
to  cause  a  still  further  removal  of  suspended 
matter  by  subsidence,  and  consequently  an 
additional  relief  to  the  sand  layer.  This  is 
possible  with  an  application  of  chemical  or 
electrolytic  treatment  sufficient  to  produce 
complete  coagulation,  because  there  will  then 
remain,  as  the  water  reaches  the  sand  layer, 
sufficient  hydrate  to  accomplish  filtration  sat 
isfactorily. 

Failure  to  provide  proper  coagulation  is  in 
admissible,  as  this  is  the  sine  qua  non  of  suc 
cessful  filtration  bv  this  method. 


The  Jewell  filter  was  operated  normally  in 
1897.  as  was  the  case  in  1895-96,  at  about 
roc  million  gallons  per  acre  daily,  equivalent 
to  1.58  gallons  per  square  foot  per  minute. 

Tn  the  last  operations  (1897)  the  only  point 
tested  in  this  connection  was  the  possibility 
of  lowering  the  rate  of  filtration  to  advantage, 
with  regard  to  a  reduction  in  the  amount  of 
coagulant  and  greater  uniformity  in  effi 
ciency,  especially  just  after  washing  the  sand 
layer.  A  comparison  of  the  efficiency  of  the 
filter  at  normal  and  half-normal  rates,  respect 
ively,  is  shown  by  the  following  representa 
tive  averages  of  leading  data  on  (1)  runs 
Nos.  67,  72,  81,  and  8_>,  and  (II)  Nos.  68,  70, 
75,  and  83: 

i  n 

Rate  of  filtration  in  million  gallons  per  acre 

daily 90-95       45-50 

Parts   per   million    of   suspended    solids    in 

river  water 181  187 

Applied  sulphate  of  alumina  in   grains  per 

gallon 1.25          i-2i 

Cubic  feet  of  filtered  water 12302       i -I  7-19 

Bacterial  efficiency 97 -2         96-6 


424 


WATER   PURIFICATION  AT  LOUISVILLE. 


Comparative  Summary. 

These  data,  with  many  others  which  are  not 
directly  comparable,  show  clearly  that,  when 
the  amount  of  coagulant  is  such  as  to  give 
at  the  normal  rate  only  a  moderately  satis 
factory  bacterial  efficiency,  a  reduction  of  the 
rate  to  one-half  of  the  normal  does  not  in 
crease  the  bacterial  efficiency,  although  it  in 
creases  slightly  the  quantity  of  water  between 
washings.  It  may  be  safely  concluded  that  a 
material  reduction  in  a  rate  of  filtration  of 
ioo  million  gallons  per  acre  daily  would  not 
diminish  the  required  amount  of  coagulant, 
and  there  would  be  no  substantial  advantages 
to  offset  the  lessened  capacity  of  the  filter. 

From  what  has  been  said  concerning  the 
proper  degree  of  coagulation  of  the  water  this 
fact  seems  to  be  almost  obvious. 

In  passing  it  may  be  stated  that,  when  by 
any  chance  the  coagulation  was  inadequate, 
it  was  repeatedly  noticed  that  with  low  rates 
the  bacterial  efficiency  and  appearance  of  the 
effluent  departed  less  from  the  normal  than  in 
the  case  of  the  regular  rate  of  filtration. 

The  evidence  presented  in  Chapter  IX  in 
dicated  that  under  suitable  conditions  the  rate 
of  satisfactory  filtration  could  be  materially 
increased  above  ioo  million  gallons  per  acre 
daily.  Our  investigations  in  1897  strength 
ened  that  view,  although  with  only  one  filter, 
and  electrical  appliances  of  too  small  capacity, 
it  was  not  considered  advisable  to  make  a 
study  of  high  rates,  especially  with  the  un- 
subsided  river  water. 

In  the  judgment  of  the  writer  it  would  be 
advisable  to  construct  a  plant  on  the  basis 
of  ioo  million  gallons  per  acre  daily,  equiva 
lent  to  435.6  square  feet  per  million  gallons 
per  24  hours,  with  the  knowledge  that  in  all 
probability  the  rate  would  be  safely  increased 
to  a  considerable  degree  in  meeting  the  de 
mand  for  a  greater  consumption  of  filtered 
water. 

Available  Head  or  Pressure  for  Filtration. 

The  total  available  head  on  the  Jewell  filter, 
as  normally  operated  by  the  Water  Company, 
was  10  feet,  of  which  5.5  feet  was  a  positive 
head  as  measured  from  the  surface  of  the 
water  to  the  bottom  of  the  sand  layer.  The 


remaining  4.5  feet  was  a  negative  head  or 
suction,  and  was  obtained  by  means  of 
a  siphon.  So  far  as  our  observation  went, 
no  necessity  for  modifying  this  head  was 
noted. 


The  claim  has  been  advanced  that  a  nega 
tive  head  possesses  a  specific  advantage 
for  economical  and  efficient  filtration.  All  the 
conditions  being  equal,  we  have  seen  nothing 
to  lead  us  to  suppose  that  there  would  be  any 
difference  in  practice  due  to  the  head  being 
either  positive  or  negative,  beyond  the  fact 
that  with  a  negative  head  there  is  ordinarily 
a  smaller  amount  of  coagulated  water  drained 
into  the  sewer  and  wasted  just  before  wash 
ing  the  sand  layer,  or  similar  operations. 

Cleaning  the  Sand  Layer  to  Relieve  Clogging. 

There  are  three  methods  which  can  be  em 
ployed  to  advantage  in  the  removal  of  accu 
mulated  matters  from  the  sand  in  order  to  re 
lieve  clogging  and  to  keep  the  sand  in  a  clean 
and  efficient  condition,  as  follows: 

1.  By   washing   the   sand    with    a   reverse 
stream  of  filtered  water  under  pressure. 

2.  By  agitation  of  the  surface  accumula 
tions  and   their  removal   into   the   sewer  by 
flushing  with  water  standing  upon  the  sand. 

3.  By  the  application  of  caustic  soda,  either 
with  or  without  steam. 

The  following  information  was  obtained 
upon  the  subject  in  1897: 

Washing. — Experience  confirmed  the  early 
conclusion  that  whenever  washing  of  the 
sand  layer  is  required  it  should  be  accom 
plished  thoroughly,  so  that  the  water  passing 
from  the  top  of  the  sand  to  the  sewer  should 
be  comparatively  clear.  In  the  Jewell  filter 
this  was  ordinarily  accomplished  with  the  aid 
of  mechanical  agitation,  by  about  600  cubic 
feet  of  wash-water  supplied  at  the  bottom  of 
the  sand  layer  at  a  pressure  of  about  7.5 
pounds.  The  rate  of  delivery  of  wash-water 
ranged  from  22  to  134,  and  averaged  71.0, 
cubic  feet  per  minute. 

Assuming  that  the  voids  in  the  normal 
sand  layer  were  35  per  cent.,  and  that  the 
thickness  of  the  layer  when  floated  was  in- 


SUMMARY  AND   DISCUSSION  OF  DATA    OF  1897. 


425 


creased  from  30  to  33  inches,  this  would  mean 
an  average  vertical  velocity  between  the  sand 
grains  of  1.37  linear  feet  per  minute. 

There  seems  to  be  no  room  for  doubt  but 
i hat  '.he  use  of  mechanical  agitation  in  the 
process  of  washing  was  a  distinct  advantage. 
In  this  case  the  teeth  of  the  agitator  extended 
to  within  three  inches  of  the  bottom  of  the 
sand  layer.  The  indications  are  that  it  would 
be  better  to  have  them  reach  as  nearly  to  the 
strainer  system  as  safety  would  allow. 

With  regard  to  the  effect  of  washing  the 
sand  layer,  upon  the  quality  of  the  effluent,  it 
will  be  recalled  that  in  1896  it  was  concluded, 
from  the  results  obtained  from  the  Warren 
and  Jewell  niters,  that  with  complete  coagula 
tion  of  the  applied  water  and  thorough  wash 
ing  of  the  sand  layer  there  was  practically  no 
diminution  in  bacterial  efficiency  following  a 
washing.  In  a  strict  sense  this  conclusion  is 
correct,  but  the  evidence  of  1897  causes  a  cer 
tain  modification  of  these  views.  '  That  is  to 
say.  when  the  coagulation  was  sufficient  to 
give  a  satisfactory  bacterial  efficiency  during 
the  latter  and  major  portion  of  a  run.  it  was 
repeatedly  found  that  the  coagulation  might 
not  be  complete  enough  to  yield  a  normal 
effluent,  bacterially,  for  some  little  time  after 
the  sand  laver  was  washed.  This  is  shown  by 
the  following  average  numbers  of  bacteria 
obtained  during  the  first  portion  of  runs  Nos. 

84.    S<J.    91.    93,    I  O2,    1O6,    122,    126,    130,    131, 

133.  142,  147.  148,  and  1 68. 

The  bacterial  efficiency  at  the  times  of  col 
lection  of  the  samples  and  the  average  num 
ber  of  bacteria  in  the  river  water  and  in  the 
effluent,  together  with  the  average  bacterial 
efficiency,  are  given.  In  preparing  this  table 
all  normal  runs  on  which  the  four  or  more 
samples  were  collected  were  averaged. 

Quantity  of  Water  Avcraee 

Filtered  between  the  .Lut 

Wash  and  the  Collection 

of  the  Sample. 

Cubic  Feet. 

15"  273 

250  225 

500  <  206 

moo  178 

Average,  river  water,  entire  run  9  970 

"         effluent,  entire  run. ...      186  98.1 

At  the  regular  rate  of  filtration  the  above 
quantities  of  water  correspond  to  6.4,  10.6, 
21.3,  and  42.5  minutes  of  service  after  filtra 
tion  was  resumed  following  a  wash. 

The  difference  between  these  figures  and 


IXiiinhci 

Bacteria 

Cubi. 


97-3 
97-7 
97-9 
98.2 


corresponding  ones  obtained  in  1896  is  ex 
plained  by  the  fact  that  in  1897  the  coagula 
tion  was  relatively  less,  as  every  effort  was 
made  to  keep  the  amount  of  coagulant  as  low 
as  was  consistent  with  good  purification. 

The  entire  evidence  taken  as  a  whole  shows 
that  when  coagulation  is  absolutely  complete 
there  is  no  appreciable  diminution  in  the 
quality  of  the  effluent  just  after  a  thorough 
washing  of  the  sand  layer. 

Nevertheless,  when  coagulation  is  very 
slightly  incomplete,  but  sufficient  to  give  sat 
isfactory  average  purification,  the  data  show 
that  just  after  washing  there  is  a  slight  dimi 
nution  in  efficiency.  This  slight  diminution 
in  efficiency,  at  this  time,  could  be  corrected 
by  an  extra  application  of  coagulant  for  a 
short  period:  by  reducing  the  rate  of  filtra 
tion,  or  by  discharging  the  effluent  at  a  nor 
mal  rate  (or  higher)  into  the  sewer  so  long  as 
it  appeared  unsatisfactory.  This  question  is 
one  which  will  have  to  be  settled  by  experi 
ence  obtained  in  practice. 

Surface  Agitation. — Surface  agitation  in  a 
manner  similar  to  that  employed  in  1896  was 
used  in  39  per  cent,  of  all  runs  on  which  the 
wash  and  waste  water  was  less  than  10  per 
cent,  of  the  filtered  water,  and  on  49  per  cent, 
of  the  runs  on  which  the  wash  and  waste  water 
did  not  exceed  10  per  cent,  of  the  filtered  water, 
and  on  which  the  average  bacterial  efficiency 
was97  per  cent,  or  over.  When  the  Jewell  filter 
was  operated  by  the  McDougall  Company  it 
was  their  custom  to  employ  surface  agitation, 
and  after  stirring  up  the  surface  accumula 
tions  to  flush  them  off  into  the  sewer  so  far 
as  practical. 

This  modification  is  one  of  merit,  although 
this  filter  was  not  constructed  in  a  manner  to 
allow  of  its  performance  in  an  entirely  satis 
factory  way.  The  reason  was  that  the  top  of 
the  inner  tank  was  about  10.5  inches  above 
the  top  of  the  sand,  and  accordingly  this  depth 
of  very  muddy  water  remained  on  the  sand 
after  the  operation  was  completed. 

The  indications  are  that  this  is  the  cheapest 
manner  of  removing  the  bulk  of  solid  matters 
from  the  surface  of  the  sand  layer,  and  it 
seems  advisable  to  modify  the  construction  of 
filters  so  that  this  procedure  can  be  employed 
to  the  greatest  advantage. 

This  would  call  for  means  of  removing  all 


426 


WATER   PURIFICATION  AT  LOUISVILLE. 


of  the  muddy  water  from  the  sand  during  or 
after  the  completion  of  the  agitation,  and 
probably  some  other  changes,  especially  in 
the  character  of  the  sand  layer. 

It  must  he  understood  that  surface  agita 
tion  could  not  completely  do  away  with  wash 
ing,  and  while  the  indications  of  its  dispensing 
in  part  wit'h  washing  are  promising,  how  far 
it  could  be  carried  into  successful  practice 
cannot  be  foretold. 

.-Implication  of  Caustic  Soda. — The  applica 
tion  of  caustic  soda  to  this  filter  on  July  3 
demonstrated  conclusively  that  it  had  a 
marked  effect  in  cleansing  the  sand  grains  of 
organic  matter  and  other  materials  attached 
to  them. 

As  niters  continue  in  service  the  use  from 
time  to  time  of  caustic  soda  would  doubtless 
be  an  advantage  in  keeping  the  sand  layer  in 
a  satisfactory  condition. 

Character  of  the  Sand  Layer. 

The  sand  layer  of  the  Jewell  filter  was  30 
inches  in  thickness  and  the  sand  grains  had 
an  effective  size  of  0.43  millimeter.  It  is  the 
judgment  of  the  writer  that  the  frictional  re 
sistance  of  the  sand  could  be  increased  to  ad 
vantage,  especially  in  an  effort  to  reduce  the 
cost  of  cleansing,  by  allowing  the  use  of  the 
partial  but  more  frequent  cleansings  by  sur 
face  agitation  in  place  of  thorough  washing 
of  the  whole  sand  layer.  This  could  be  ac 
complished  by  increasing  the  thickness  of  the 
layer  or  by  using  a  sand  with  a  finer  grain,  or 
both.  The  indications  are  that  this  could  be 
done  best  bv  maintaining  the  thickness  of  the 
sand  layer  at  30  inches,  and  using  a  finer 
sand. 

It  is  recommended  that  a  sand  be  employed 
having  an  effective  size  of  about  0.35  milli 
meter.  As  the  resistance  of  the  sand  to  the 
How  of  water  varies  inversely  as  the  square 
of  the  effective  size,  this  would  increase  the 
friction  in  the  ratio  of  2  to  3. 

SECTION  No.   n. 

QUALITY  OF  THE  EFFLUENT  AFTER  PROPER 
SEDIMENTATION,  COAGULATION,  AND 
FILTRATION  —  INDEPENDENT  OF  THE 
NATURE  OF  THE  COAGULANT. 

Under  suitable  conditions  for  economical 
and  efficient  treatment,  as  noted  above,  the 


quality  of  the  Ohio  River  water  after  purifi 
cation  is  presented  in  the  following  para 
graphs.  It  will  be  noted  that  the  statements 
in  this  section  are  independent  of  the  nature 
of  the  coagulants.  Following  this  the  effect 
of  the  several  available  coagulants  is  dis 
cussed. 

Appearance. 

The  appearance  of  the  Ohio  River  water 
after  purification  under  the  above  conditions 
was  very  satisfactory,  as  it  was  practically 
free  from  turbidity  and  color. 

Taste  and  Odor. 

As  a  rule  the  taste  of  the  effluent  was  some 
what  different  from  that  of  the  river  water, 
in  that  the  earthy  taste  due  to  suspended 
earthy  matters  in  the  unpurified  water  was  re 
moved.  The  odor  of  the  effluent  was  the  same 
as  before  purification,  and  was  never  found  to 
be  sufficient  to  be  in  any  way  objectionable. 

Organic  Matter. 

The  amount-  of  organic  matter  remaining 
in  the  effluent  was  found  to  range,  when  ex 
pressed  as  nitrogen  in  the  form  of  albuminoid 
ammonia,  from  .030  to  .110  part  per  million, 
and  averaged  about  .070  part,  expressed  as 
oxygen  consumed  the  range  was  from  0.5  to 
1.6  parts,  and  the  average  was  i.o  part. 

In  such  small  amounts  the  organic  matter 
in  the  effluent  was  entirely  unobjectionable. 

Mineral  Matter. 

Upon  purification  the  changes  in  the  min 
eral  contents  of  the  Ohio  River  water  is  char 
acterized  chiefly  by  the  complete  removal  of 
suspended  mud,  silt,  and  clay.  This  is  un 
questionably  an  advantage,  although  from  a 
sanitary  standpoint  the  evidence  indicates 
that  such  an  action  does  not  specifically  im 
prove  the  healthfulness  of  the  water,  except 
perhaps  in  the  case  of  some  abnormal  indi 
viduals. 

From  an  industrial  point  of  view  the  re 
moval  of  suspended  mineral  matter  is  dis 
cussed  below. 


SUMMARY  AND  DISCUSSION   OF  DATA     OF  1807. 


427 


With  regard  to  the  dissolved  mineral  con 
stituents  of  the  effluent,  they  do  not  differ 
materially  from  those  of  the  river,  except  as 
influenced  by  the  nature  of  the  coagulants  as 
shown  in  the  next  section. 

Gases. 

The  principal  gases  in  the  river  water,  car 
bon  dioxide  (uniting  with  water  to  form 
free  carbonic  acid)  and  atmospheric  oxygen, 
were  practically  unaffected  by  purification  ex 
cept  through  the  nature  of  the  coagulant. 

Alg(c  and  other  Grosser  Micro-oganisms. 

It  was  found  that  the  effluent  was  practi 
cally  free  from  all  diatoms,  alga?,  and  other 
micro-organisms  which  may  be  called  large 
when  compared  with  bacteria. 

Bacteria. 

Under  favorable  conditions  of  coagulation 
and  filtration  the  bacteria  in  the  effluent  were 
reduced  to  a  point  which  was  satisfactory  in 
the  light  of  modern  sanitary  science. 

Undecomposed  Coagulants. 

This  topic  is  entered  into  in  subsequent 
sections,  and  the  conditions  of  proper  coagu 
lation  as  stated  above  in  the  title  lead  to  the 
inference  that  the  presence  of  Undecomposed 
coagulants  in  the  effluent  is  not  a  factor  for 
consideration.  For  the  sake  of  explicitness, 
however,  it  may  be  mentioned  here  that,  with 
suitable  conditions  for  the  employment  of 
subsidence  to  its  economical  limit,  with  com 
mercial  sulphates  there  would  be  no  occasion 
for  the  chemicals  to  be  applied  in  amounts 
exceeding  that  capable  of  complete  decom 
position  by  the  river  water.  Concerning  the 
use  of  electrolytically  formed  iron  hydrate,  it 
is  not  probable  that  dissolved  iron  would  ever 
appear  in  the  effluent;  although  it  is  possible 
that  large  amounts  of  clay  in  the  river  water 
in  midsummer,  when  the  amount  of  dissolved 
atmospheric  oxygen  in  the  water  is  least, 
might  press  closely  and  perhaps  overreach 
the  safe  limit  in  the  amount  of  iron  which 
could  be  completely  oxidized  and  rendered 


insoluble.  If  such  an  occasion  should  arise 
it  would  be  of  very  short  duration  and  could 
be  obviated  by  the  use  of  small  amounts  of 
commercial  sulphates  to  supplement  the  elec 
trolytic  process. 

In  1897  there  was  no  instance  where  any 
difficulty  was  experienced  in  keeping  the 
effluent  free  from  Undecomposed  coagulants. 

Storage  of  the  Effluent. 

The  conditions  of  successful  practice  de 
mand  that  between  the  purification  plant  and 
the  distributing  pipes  there  should  be  provid 
ed  a  reservoir  in  which  sufficient  filtered  water 
may  be  stored  to  compensate  for  all  inequali 
ties  in  the  rate  of  consumption  at  different 
hours  of  the  day,  and  also  to  allow  the  plant 
to  be  stopped  when  repairs,  etc.,  require  it. 
The  question  of  storage  of  the  effluent  is  one 
of  much  practical  importance. 

While  it  is  true  that  the  effluent  as  it  leaves 
the  filter  is  free  from  algae,  diatoms,  etc., it  is  a 
fact  that  the  spores  of  these  micro-organisms 
are  present  in  the  atmosphere;  and  the  fil 
tered  water  contains  a  considerable  amount 
of  food  (principally  in  the  form  of  nitrates) 
for  the  growth  of  these  organisms,  many  of 
which  give  rise  to  objectionable  tastes  and 
odors.  The  growth  of  these  organisms  re 
quires  the  presence  of  sunlight;  and  the  effect 
of  purification  is  marked  in  this  respect,  be 
cause  in  open  reservoirs  the  removal  of  all 
suspended  matters  from  the  water  permits  the 
sun's  rays  to  penetrate  the  filtered  water, 
while  with  the  river  water  this  is  impossible. 
This  was  demonstrated  conclusively  by  mi 
croscopical  examinations  of  the  river  water 
with  different  amounts  of  suspended  matter 
in  it  during  warm  weather  (the  period  of 
maximum  growth  of  these  organisms),  as 
shown  in  Chapter  I. 

To  estimate  the  period  of  storage  during 
which  the  filtered  water  might  be  stored  in 
open  reservoirs,  before  the  growth  of  algae 
would  begin  in  warm  weather,  is  a  difficult 
matter.  It  would  vary  widely  with  the  tem 
perature  and  the  frequency  of  sunshiny  days, 
the  amount  and  specific  character  of  the  par 
ticles  of  floating  matter  coming  from  the  at 
mosphere,  and  the  amount  of  dissolved  mat 
ter  in  the  filtered  water,  adaptable  as  food  for 


4z8 


WATER  PURIFICATION  AT  LOUISVILLE. 


these  organisms.  Inspection  of  isolated  por 
tions  of  the  Ohio  River  where  the  current 
was  almost  nil,  lead  to  the  belief  that  sudh  a 
growth  mig'ht  occur  in  much  less  than  one 
week.  General  information  concerning  the 
life  history  of  these  organisms  indicates  that 
at  times  the  period  would  be  as  short  as  4  j 
days,  but  it  is  possible  that  under  some  cir 
cumstances  it  might  be  no  longer  than  2  days. 
It  is  certain,  however,  that  it  would  not  be 
safe  to  expose  the  filtered  water  to  the  rays 
of  the  sun  for  an  average  period  of  about  6 
days,  as  would  be  the  case  if  the  uncovered 
reservoir  at  Crescent  Hill  were  used  under 
present  conditions. 

Difficulties  with  alga;  growths  may  be 
obviated  by  making  the  period  of  exposure 
to  the  sun's  rays  very  short,  or  by  using  a 
covered  reservoir,  or  both.  The  covered  res 
ervoir  would  be  safest,  especially  as  it  would 
preclude  trouble  from  growths  of  organisms 
which  might  become  seeded  upon  the  walls 
of  the  reservoir. 

Corrosion  by  the  Effluent  of  Metal  Receptacles. 

i 

This  subject  was  discussed  in  Chapter  IX, 
but  in  1897  additional  information  of  value 
was  obtained. 

In  all  probability  there  would  be  no  diffi 
culty  whatever  in  the  action  of  the  effluent 
upon  lead  pipes,  or  iron  pipes  which  were 
properly  coated  with  a  protective  paint.  With 
uncoated  iron  pipes  or  receptacles,  especially 
those  of  wrought  iron,  the  effluent  would 
have  an  increased  corroding  action.  As  al 
ready  explained,  water  normally  produces 
corrosion  by  the  joint  action  of  the  carbonic 
acid  and  the  atmospheric  oxygen  dissolved  in 
the  water.  This  action  produces  iron  (ferric) 
hydrate,  just  as  in  the  Anderson  process  of  se 
curing  coagulation.  When  first  formed,  iron 
hydrate  is  flocculent  and  fairly  porous,  and  it 
will  be  understood  from  what  has  been  said 
concerning  the  nature  of  this  compound  as  a 
coagulant,  that  it  has  the  power  of  incorporat 
ing  within  itself  suspended  matters  and  some 
dissolved  matters.  The  resulting  mass  is 
much  less  porous  than  when  no  suspended 
matters  are  embodied  in  the  hydrate. 
Facts  show  that  this  is  of  practical  import 
ance  in  the  consideration  of  corrosion  by 


the  Ohio  River  water  before  and  after  purifi 
cation. 

Partial  Protective  Influence  of  Suspended 
Matter  against  Corrosion. — Comparison  of  the 
rc'ative  corroding  action  of  the  Ohio  River 
water  before  and  after  the  removal  of  silt  and 
c'ay,  by  filtration  through  filter-paper,  a  Pas 
teur  filter  or  other  device  in  which  the  chem 
ical  character  of  the  dissolved  compound  would 
not  be  materially  changed  in  quality  or  amount, 
showed  repeatedly  and  without  exception 
that  the  suspended  matter  acted  as  a  partial 
protection  to  the  iron.  This  is  illustrated  by 
the  following  representative  experiment,  in 
which  8  pieces  of  o. 5-inch  wrought-iron  rods 
weighing1  150  grams  were  placed  in  2200 
cubic  centimeters  of  river  water  (chemical 
sample  No.  985)  and  the  effluent  after  pass 
ing  this  water  through  a  Pasteur  filter.  The 
experiment  was  continued  for  ten  days,  and 
in  order  that  the  effluent  might  not  be  dis 
similar  to  practical  conditions  by  an  exhaus 
tion  of  carbonic  acid  and  oxygen,  air  (con 
taining  these  gases)  was  constantly  passed 
through  each  water.  At  the  end  of  this  ex 
periment  it  was  found  that  in  the  case  of  the 
river  water  i.i  grams  of  iron  had  been  lost 
from  the  rods  by  corrosion,  while  in  the  efflu 
ent  the  corresponding  amount  was  2.  i  grams. 
To  prove  that  this  was  not  due  essentially  to 
an  action  of  dissolved  chemical  compounds 
(exclusive  of  course  of  carbonic  acid  and 
oxygen),  this  experiment  was  repeated  for  14 
days,  using  distilled  water  with  10  parts  of 
common  salt  in  each  bottle,  and  in  one  of 
them  some  fine  clay  (kaolin)  was  suspended. 
The  results  show  that  in  the  case  with  sus 
pended  clay  there  was  a  loss  of  iron  by  cor 
rosion  of  0.90  milligram,  while  in  the  clear 
water  the  iron  lost  1.81  milligrams. 

Bearing  in  mind  the  decisive  proof  that  on 
a  laboratory  scale  the  suspended  matter  gave 
a  marked  although  incomplete  protection  to 
iron  from  corrosion  by  the  water,  an  exam 
ination  was  made  of  the  experience  of  this 
Company  in  the  corrosion  of  uncoated  pipes. 
The  most  notable  instance  of  the  slowness 
with  which  the  Ohio  River  water  corrodes 
uncoated  iron  is  in  the  case  of  the  intake  at 
the  old  pumping  station.  This  wrought-iron 
pipe.  0.37  inch  thick  and  50  inches  in"  diam 
eter,  was  put  in  service  in  1860,  and  remained 


SUMMARY  AND   DISCUSSION  OF  DATA    OF  1897. 


429 


in  continuous  service  without  any  artificial 
protective  coating  until  1894.  After  34  years 
of  exposure  to  the  river  water  it  was  corroded 
to  a  considerable  degree,  but  not  enough  to 
warrant  its  removal,  and  it  was  coated  with  a 
layer  of  cement  and  continued  in  service. 

In  concluding  it  may  be  stated  that  the  rea 
son  that  the  effluent  has  a  greater  corroding 
action  upon  iron  than  has  the  river  water,  is 
because  the  suspended  matters  mixing  with 
the  hydrate  diminish  materially  the  contact 
of  the  water  with  the  surface  of  the  bright 
metal  at  the  point  of  corrosion.  In  a  measure 
this  effect  is  similar  to  that  in  the  case  of  lead 
pipes.  The  Ohio  River  water  dissolves  new 
bright  lead  rapidly,  but  with  great  prompt 
ness  it  forms  a  very  thin  layer  of  basic  carbon 
ate  of  lead  which,  practically  speaking,  is 
absolutely  impervious  to  water  and  conse 
quently  arrests  all  further  action. 

Adaptability  of  Effluent  for  Boiler  Use. 

Compared  with  the  average  boiler  waters  in 
this  section  of  the  country,  and  farther  West, 
the  Ohio  River  water  in  an  unpurified  condi 
tion  is  a  fairly  satisfactory  water  for  use  in 
steam-boilers.  In  comparison  with  the  clear 
and  soft  waters  in  the  East,  however,  it  has 
t\vo  marked  disadvantages. 

In  the  first  place,  during  the  greater  part 
of  the  year  the  amount  of  suspended  matter 
is  so  great  that  it  forms  large  quantities  of 
sludge,  which  at  times  cannot  be  removed  by 
"  blowing  off,"  so  that  it  is  necessary  to  enter 
the  boiler  and  remove  it  by  manual  labor. 
At  such  times  the  incrusting  constituents  are 
very  low  in  amount  and  are  deposited  upon 
the  separate  particles  of  the  sludge  for  the 
most  part,  and  seem  to  leave  the  metal  al 
most  free  from  sulphate  of  lime,  etc.  The  re 
moval  of  these  large  amounts  of  suspended 
matterj  would  be  an  advantage,  unquestion 
ably,  and  the  effluent  would  therefore  be  su 
perior  to  the  river  water. 

The  second  disadvantage  of  the  river  water 
for  use  in  boilers  is  seen  at  times  of  very  low 
water  in  the  river,  such  as  is  found  during  the 
fall  months.  At  these  times  the  water  con 
tains  not  only  sulphate  of  lime  and  other  in- 
crusting  constituents  in  considerable  quanti 
ties  (and  far  in  excess  of  the  average 


amounts),  but  also  some  very  fine  clay.  In 
boilers  this  clay  and  the  incrusting  con 
stituents  unite  and  form  a  coating  resembling 
cement,  which  is  very  difficult  to  remove 
from  the  surface  of  the  boiler.  The  removal 
of  the  suspended  clay  from  the  water  before 
its  entrance  into  boilers  would  therefore  im 
prove  the  water  for  boiler  use. 

With  regard  to  the  dissolved  chemical  com 
pounds  such  as  incrusting  constituents,  there 
is  no  difference  between  the  river  water  and 
the  effluent,  independent  of  the  nature  of  the 
coagulant.  Disregarding  the  influence  of  the 
coagulant,  which  is  discussed  beyond,  the 
effluent  is  more  suitable  for  boiler  use  than  is 
the  river  water. 

Uniformity  in  Quality  of  Effluent. 

With  proper  conditions  for  sedimentation, 
coagulation,  and  filtration,  and  independent  of 
the  nature  of  the  coagulant,  there  ought  not, 
and  need  not,  be  any  objectionable  variations 
in  the  quality  of  the  effluent  in  consequence  of 
the  purification.  It  was  found  that  the  qual 
ity  of  the  effluent  does  vary  owing  to  the  in 
herent  variations  in  the  river  water.  From  a 
practical  point  of  view  these  variations  would 
occur  in  the  dissolved  mineral  compounds, 
especially  the  carbonic  acid  and  the  incrust 
ing  constituents.  The  evidence  obtained  in 
1897  showed  that  with  regard  to  these  con 
stituents  the  composition  of  the  river  water 
is  more  variable  than  was  considered  to  be 
the  case  in  1896.  The  normal  and  extreme 
amounts  of  carbonic  acid  and  incrusting  con 
stituents  in  parts  per  million  in  the  river  water 
are  as  follows: 


Carbonic  acid 133 

Incrusting  constituents 51 

SECTION  No.  12. 


MANNER   IN   WHICH   THE   NATURE   OF  THE 

COAGULANT  AFFECTED  THE  QUALITY 

OF  THE  EFFLUENT. 

There  are  three  different  coagulants,  each  of 
a  somewhat  different  nature,  which  have  been 
considered  as  factors  in  this  problem,  namely: 
sulphate  of  alumina,  persulphate  of  iron,  and 
electrolytically  formed  iron  hydrate.  As 


43° 


WATER  PURIFICATION  AT  LOUISVILLE. 


stated  in  Chapter  III,  the  passage  of  unde- 
composed  sulphates  into  the  effluent  would 
not  only  be  inadmissible,  but  inexcusable. 
Our  experience  in  1897  allows  of  no  modifi 
cation  of  this  view.  It  may  be  mentioned  in 
passing,  however,  that  the  presence  of  unde- 
composed  sulphates  in  the  effluent  would  be 
exceedingly  objectionable  in  connection  with 
corrosion.  With  regard  to  the  electrolytic 
iron  method  there  would  be  no  danger  of  any 
iron  getting  into  the  effluent  during  cold 
weather,  but  in  midsummer  if  a  heavy  rise  in 
the  river  should  occur  there  might  not  be 
sufficient  oxygen  in  the  water  to  convert  all 
the  iron  into  insoluble  ferric  hydrate.  Under 
these  circumstances  it  would  be  necessary  to 
supplement  the  safe  limit  in  this  treatment 
with  some  other  coagulant,  or  to  aerate  the 
water. 

In  view  of  the  fact  that  it  is  practicable 
to  coagulate  this  water  properly  without  the 
passage  of  undecomposed  sulphates  or  of  dis 
solved  hydrates  into  the  effluent,  and  that  the 
necessity  for  doing  so  is  imperative,  we  will 
consider  the  nature  of  the  effect  of  the  several 
coagulants  upon  the  quality  of  the  effluent 
only  when  applied  in  permissible  (but  ade 
quate)  amounts. 

In  general  terms  the  quality  of  the  effluent 
is  affected  in  two  ways  by  the  nature  of  the 
coagulant:  first,  with  regard  to  the  amount 
of  oxygen  and  carbonic  acid;  and,  second, 
with  reference  to  the  increase  in  amount  of 
incrusting  constituents  in  consequence  of  the 
lime  and  magnesia  passing  from  the  (alkaline) 
carbonates  and  bicarbonates  into  the  neutral 
sulphates. 

From  a  sanitary  point  of  view  there  is  no 
reason  to  believe  that  these  factors  under  suit 
able  conditions  of  practice  would  be  of  any 
practical  importance.  They  would  influence, 
however,  the  corroding  and  incrusting  power 
of  the  effluent. 

The  manner  in  which  the  several  available 
coagulants  affect  the  quality  of  the  efflu 
ent,  expressed  quantitatively  in  equivalent 
amounts  of  i  grain  per  gallon  of  sulphate  of 
alumina  containing  9.87  per  cent,  of  alumi 
num,  is  shown  in  the  table  opposite. 

In  order  to  consider  the  practical  effect  of 
the  nature  of  the  coagulant  upon  the  corrod 
ing  and  incrusting  power  of  the  water,  it  is 


Coagulant. 

Oxygen. 

Alkalinity. 

Constituents. 

Dioxide. 

Sulphate  of 

None 

9.04 

9.04 

3-97 

alumina 
Persulphate 

(decrease) 
u.  -8 

(increase) 
11.78 

(increase) 
5-16 

of  iron 

(decrease) 

(increase) 

(increase) 

Electrolytic 
iron 

0.76 
(decrease) 

None 

None 

None 

COMPARATIVE  EFFECT  UPON  THE  QUALITY 
OF  THE  EFFLUENT  OF  ONE  GRAIN  PER 
GALLON  OF  SULPHATE  OF  ALUMINA,*  AND 
ITS  EQUIVALENT  OF  OTHER  COAGULANTS. 

(Changes  in  Constituents  of  Effluent  expressed  in  Parts  per 
Million.) 


.87   pe 


necessary  to  know  the  amount  of  the  above 
changes.  This  depends  upon  the  amounts  of 
coagulants  used,  and  the  estimated  quantities 
of  coagulants  which  would  be  required  are 
presented  in  the  next  section.  In  section 
No.  14  the  degree  to  which  the  several  co 
agulants  would  affect  the  effluent  is  shown 
and  its  practical  significance  discussed. 

SECTION  No.  13. 

AMOUNTS  OF  THE  DIFFERENT  AVAILABLE 
COAGULANTS  WHICH  WOULD  BE  RE 
QUIRED,  WITH  OPTIMUM  CONDITIONS 
OF  SUBSIDENCE  AND  FILTRATION,  TO 
PURIFY  SATISFACTORILY  THE  OHIO 
RIVER  WATER. 

Taking  into  consideration  the  employment 
to  their  economical  limits  of  plain  subsidence 
and  an  extended  but  varying  period  of  sub 
sidence  with  coagulation,  and  in  some  cases 
a  division  in  the  application  of  coagulants,  it 
is  estimated  that  the  annual  average  amounts 
of  required  coagulants  for  the  satisfactory 
purification  of  the  Ohio  River  water  would 
be  as  follows: 

ESTIMATED  REQUIRED  AMOUNT  OF  COAGULANT 
PER   GALLON    OF    RIVER    WATER. 

Coagulant.                                     Max.  Min.  Aver. 

Grains  of  sulphate  of  alumina* 4.00  0.75  1.75 

Grains  of  sulphate  of  iron  f 4.00  0.75  1.75 

Ampere-hour  of  electric  current  on  iron 

electrodes 0.16  0.03  0.07 


The  average  amount  of  coagulant  in  the 
respective  equivalent  forms  would  probably 
range  according  to  the  rainfall  and  other  con 
ditions  in  amounts  from  1.50  to  2.00  grains 


SUMMARY  AND   D/SCUSSION   OF  DATA    OF  1897. 


43' 


in  the  case  of  the  sulphates,  and  from  0.06 
to  0.08  ampere-hour  of  electric  current 
on  iron  electrodes.  The  mean  average  is 
given  above. 

In  regard  to  the  maximum  amount  of  elec 
trolytic  iron  treatment  it  is  to  be  borne  in 
mind  that  the  amount  above  given  could  only 
be  safely  applied  at  times  when  the  amount  of 
oxygen  dissolved  in  the  river  water  was  rela 
tively  large.  As  a  rule,  the  maximum  amount 
of  electrolytic  treatment  which  could  be  safely 
applied  would  be  about  o.  12  ampere-hour  per 
gallon. 

SECTION  No.  14. 

DEGREE  TO  WHICH  THE  SEVERAL  COAGU 
LANTS  IN  THEIR  RESPECTIVE  AMOUNTS 
WOULD  AFFECT  THE  QUALITY  OF  THE 
EFFLUENT,  WITH  ITS  PRACTICAL  SIG 
NIFICANCE  AND  A  CONSIDERATION  OF 
THE  ADVISABILITY  AND  COST  OF  THE 
REMOVAL  OF  THE  ADDED  CONSTITUENTS. 

Taking  the  annual  average  amounts  of  the 
required  coagulants  as  estimated  in  the  last 
section,  the  amount  of  changes  in  the  several 
constituents  of  the  effluent  which  would  ac 
tually  occur  may  be  taken  as  follows: 

CHANGES  IN  CONSTITUENTS  OF  RIVER  WATER. 
(Parts  per  Million.) 


in  Oxyeen. 


in  Alkalinity. 


The  first  step  in  the  consideration  of  the 
practical  significance  of  these  data  is  to  note 
the  range  of  these  constituents  as  they  natu 
rally  occur  in  the  Ohio  River  water, 


ANNUAL  RANGES  OF  AFFECTED  CONSTITU 
ENTS  AS  THEY  NATURALLY  OCCUR  IN  THE 
OHIO  RIVER  WATER. 

(Parts  per  Million.) 


Alkalinity. 


4.6  8.6     !       1080     !     21.0     I     65.0 


Incrusting  Constituents 


Carbon  Dioxide.* 


2<J.O  70.0 


Coagulant. 











Max. 

Min. 

Av. 

Max. 

Min. 

Av. 

Sulphate    of 

alumina  .... 

None 

None 

None 

27.0        6  .  o 

12.5 

Persulphate  of 

None 

7   8 

Electrolytic 

! 

Increase  in  IncrustinR           Increase  in  Cnrbon 

Constituents.                            Dioxide. 

Coagulant. 

Max. 

Min. 

Av. 

Max. 

Min. 

Av. 

Sulphate    of 

alumina  .... 

27.0 

6.0 

12.5 

II.  g 

2.6 

5-5 

Persulphate  of 

7  8 

16  2 

Electrolytic 

None 

None 

None 

None 

None 

None 

Atmospheric  Oxygen — Electrolytic  Iron  Process. 

The  atmospheric  oxygen  dissolved  in  the 
water  is  affected  only  in  the  electrolytic  iron 
process.  It  will  be  seen  that  while  the  aver 
age  decrease  in  oxygen  is  equal  to  less  than 
half  the  average  amount  in  the  river  water, yet 
the  maximum  (calculated)  decrease  is  nearly 
double  the  minimum  amount  in  the  water. 
Owing  to  the  influence  of  temperature  the 
amount  of  oxygen  in  the  water  is  least  during 
the  summer  months.  During  cold  weather 
the  indications  are  that  there  would  be 
enough  oxygen  for  the  satisfactory  use  of  this 
process.  An  exhaustion  of  the  oxygen  and 
the  passage  of  soluble  iron  into  the  filtered 
water  is  inadmissible.  Such  a  state  of  affairs 
would  probably  never  occur  except  at  times 
when  the  river  water  might  be  heavily 
charged  with  clay  in  midsummer.  To  guard 
against  this  effectively  it  would  be  necessary 
to  provide  facilities  for  the  use  of  sulphates 
to  supplement,  at  times  in  hot  weather,  the 
electrolytic  iron  process. 

With  regard  to  alkalinity,  incrusting  con 
stituents,  and  carbonic  acid,  they  remain  un 
affected  by  the  electrolytic  iron  process. 

Changes  in  Alkalinity,  Incrusting  Constituents, 
and  Carbonic  Acid — Process  with  Com 
mercial  Sulphates. 

The  above  data  show  that  in  this  process 
the  atmospheric  oxygen  is  unaffected,  while 
the  alkalinity  is  reduced  and  the  incrusting 
constituents  and  carbonic  acid  increased.  In 
the  case  of  persulphate  of  iron  the  changes 


432 


WATER   PURIFICATION  AT  LOUlSVILLh. 


are  30  per  cent,  greater  than  with  sulphate 
of  alumina,  other  conditions  being"  equal.  In 
view  of  the  fact  that  the  two  sulphates  are  of 
about  equal  cost,  the  sulphate  of  alumina  is 
therefore  the  better  chemical  to  employ  as  a 
coagulant.  As  stated  and  explained  in  Chap- 
tor  111,  the  use  of  this  product  in  such 
amounts  that  it  would  pass  through  the  filter 
in  an  undecomposed  form  would  not  only  be 
inadmissible  but  inexcusable. 

\Ye  shall  therefore  consider  sulphate  of  alu 
mina  more  especially  in  the  balance  of  this 
section,  but  will  take  up  the  effect  of  each  sul 
phate  in  the  following  connection: 

1.  Sanitary  character  of  effluent  in  this  re 
gard. 

2.  Use  of  soap. 

3.  Incrustations  and  adaptability  for  use  in 
steam-boilers. 

4.  Corrosion  of  iron  receptacles. 

5.  Corrosion  of  lead  receptacles. 

Effect  upon  the  Sanitary  Character  of  Effluents 

due  tn  Changes  Caused  by  the  Use  of 

Sulphates. 

So  far  as  \ve  have  been  able  to  learn  the 
sanitary  character  of  the  effluent  would  not 
be  appreciably  affected  by  the  reductions  in 
the  alkalinity  and  the  corresponding  increases 
iu  incrusting  constituents  and  carbonic  acid. 
within  the  ranges  noted  above.  There  is  no 
reason  to  believe  that  the  carbonic  acid  has 
any  significance  in  this  respect,  and  we  have 
only  to  consider  the  effect  of  changing  the 
lime  (and  some  magnesia)  from  the  carbonate 
to  the  sulphate.  In  this  connection  it  is  to  be 
noted  that  during  the  greater  part  of  the  year 
the  amount  of  sulphate  of  lime  in  the  chem 
ically  treated  effluent  would  be  far  less  than 
is  naturally  present  in  the  river  water  during 
the  fall  months.  And  at  that  season  of  the 
year  the  percentage  increase  of  sulphate  of 
lime  due  to  applied  chemicals  would  be  very 
small. 

Effect  upon  the  Amount  of  Soap  Required  by 

the  Filtered  Water  due  to  Changes  Caused 

by  the  Use  of  Sulphates. 

The  amount  of  soap  required  by  a  water 
for  washing  purposes  depends  upon  the  total 


amount  of  lime  and  magnesia  present  in  the 
water.  This  is  indicated  by  the  total  hard 
ness  of  the  water,  which  is  measured  by  the 
sum  of  the  alkalinity  and  incrusting -constitu 
ents,  approximately  equal  to  the  temporary 
and  permanent  hardness,  respectively.  As 
the  decrease  in  alkalinity  and  increase  in  in- 
crusting  constituents  are  proportional,  the 
soap  consuming  power  would  be  constant 
under  ordinary  conditions. 

After  prolonged  boiling  of  the  filtered 
water  it  would  require  slightly  more  soap,  be 
cause  upon  the  expulsion  of  carbonic  acid  gas 
there  would  be  less  lime  in 'the  form  of  car 
bonate  to  settle  out  than  in  the  case  of  the 
river  water. 

Changes  in  Adaptability  of  the  Effluent  for  Use 

in  Steam-boilers  due  to  tlte  Employment 

of  Sulphates  as  Coagulants. 

The  adaptability  of  a  water  for  boiler  use, 
independent  of  matters  in  suspension,  is  gov 
erned  by  the  amounts  of  incrusting  constitu 
ents,  and  in  this  respect  the  two  sulphates  in 
question  produced  relative  changes  substan 
tially  as  follows: 

PERCENTAGE  INCREASE  OF  INCRUSTING  CON 
STITUENTS  OF  THE  EFFLUENT  ABOVE  THOSE 
IN  THE  RIVER  WATER. 


Ma: 


Mi 


With  sulphate  of  alumina. . 
With  persulphate  of  iron. . 


300 
400 


"7° 
90 


Owing  to  the  fact  that  the  increase  in  the 
incrusting  constituents  is  low  when  the 
amounts  naturally  present  in  the  river  water 
are  high  (fall  months)  the  maximum  amount 
in  the  filtered  water  as  shown  by  these  data 
would  not  be  far  in  excess  of  that  in  the  river 
water. 

COMPARISON  OF  THE  MAXIMUM  AND  AVER 
AGE  AMOUNTS  OF  INCRUSTING  CONSTITU 
ENTS  OF  THE  EFFLUENT  AND  OF  THE  RIVER 

WATER. 

(Parts  per  Million.) 

Maximum        Avpratrp 
maximum.      rtVLr.i^i. 

Ohio  rievr  water 51  18 

Effluent  with  sulphate  of  alumina 57  30 

Effluent  with  persulphate  of  iron 59  35 

From  the  above  figures  it  is  seen  that  the 
average  annual  amount  of  incrusting  con 
stituents  in  the  effluents  when  sulphate  of  alu 
mina  and  persulphate  of  iron  are  used  are 
only  60  and  70  per  cent.,  respectively,  of  the 


SUMMARY  AND   DISCUSSION  OF  DATA    OF  1807. 


433 


maximum  amount  naturally  present  in  the 
Ohio  River  water,  and  at  times  when  the  river 
water  is  least  suitable  for  use  in  boilers  the 
increase  in  incrusting  constituents  is  only 
12  and  16  per  cent.,  respectively. 

These  additions  in  incrusting  constituents 
cannot  be  regarded  as  other  than  undesirable, 
hut  it  is  finite  possible,  if  not  probable,  that 
the  practical  effect  of  the  additions  when 
proper  subsidence  is  availed  of.  would  be  off 
set  by  the  freedom  of  the  effluent  from  sus 
pended  matters.  Experience  alone  can 
demonstrate  this  conclusively. 

There  is  another  way  of  looking  at  the  ap 
plicability  of  the  effluents  obtained  with  com 
mercial  sulphates  in  connection  with  use  in 
boilers.  That  is  to  compare  these  data  with 
the  available  results  showing  the  incrusting 
constituents  (permanent  hardness)  of  the 
water  supplies  of  other  cities.  So  far  as  they 
were  available  these  data  are  as  follows: 
COMPARISON  OF  INCRUSTING  CONSTITUENTS 

(PERMANENT     HARDNESS)    OF    THE    WATER 

SUPPLIES   OF    VARIOUS    CITIES. 
(Parts  per  Million.) 

Supply.                                                          ronstituenis. 
Unfiltered  Ohio  River  water  (average),  Louis 
ville,  Ky 18 

Filtered   Ohio  River   water   with    sulphate   of 

alumina,  Louisville,  Ky 3" 

Filtered  Ohio  River  water  with  persulphate  of 

iron,  Louisville,  Ky 35 

Lynn    Mass 4 

Holyoke,    Mass 18 

New  York.    N.  Y I? 

Scranton,   Pa °4 

Cincinnati,   O 20 

St.  Louis,  Mo 48 

London,   England 5° 

Liverpool,   England    57 

Manchester,    England 19 

Bradford,  England 21 

Birmingham,    England 64 

Glasgow,  Scotland 9 

Paris,  France 3° 

Geneva,  Switzerland 53 

Vienna,  Austria 2O 

St.  Petersburg,  Russia 4° 

With  regard  to  the  amounts  of  incrusting 
constituents  in  the  water  supplies  of  other 
cities  it  is  not  known  how  widely  they  may 
vary.  The  data  are  averages  of  all  available 
results  from  reliable  sources,  but  as  a  rule 
only  one  figure  was  given  in  a  single  work. 
In  the  case  of  most  of  the  European  results 
the  figures  appear  to  be  given  as  representa 
tive  ones,  and  it  is  believed  that  they  suffice 
for  the  present  purpose. 

While  the  above  evidence  shows  that  the 
Ohio  River  water,  after  purification  in  which 


plain  subsidence  preceded  coagulation  with 
sulphate  of  alumina  or  persulphate  of  iron, 
would  not  be  an  especially  soft  water  as 
viewed  by  Eastern  standards,  yet  as  com 
pared  with  the  waters  of  the  Western  part  of 
this  country  it  would  not  be  an  objectionable 
one,  nor  would  this  factor  be  of  sufficient 
weight  to  offset  the  advantages  of  filtration. 

Furthermore,  it  is  possible  to  remove  these 
incrusting  constituents  from  the  water  by  the 
application  of  caustic  soda  followed  by  sub 
sidence  or  filtration.  On  the  basis  of  $1.85 
per  100  pounds  for  caustic  soda,  containing 
60  per  cent,  available  sodium  oxide,  the  cost 
of  chemical  per  million  gallons  of  water  to 
remove  i  part  per  million  of  incrusting  con 
stituents  would  be  12  cents. 

In  the  judgment  of  the  writer  this  step 
would  not  be  justifiable  so  far  as  the  entire 
supply  is  concerned,  and  it  is  hardly  probable 
that  it  would  be  worth  while  for  large  manu 
facturing,  establishments  to  adopt  it. 

Corrosion  of  Iron  Receptacles  due  to  Changes  in 
the  Effluent  Caused  by  the  Use  of  Sul 
phates  as  Coagulants. 

It  has  already  been  explained  in  detail  that 
corrosion  of  uncoated  iron  is  due  chiefly  to 
carbonic  acid  and  dissolved  oxygen  in  a 
water;  and  in  1897  it  was  learned  that  the 
degree  of  corrosion  by  the  water  would  be 
greater  after  purification  due  simply  to  the  re 
moval  of  the  suspended  matter  which  served 
in  a  measure  as  a  protective  coating.  With 
adequate  facilities  for  the  proper  employment 
of  subsidence,  the  amount  of  applied  sulphate 
could  be  reduced  much  below  that  employed 
at  times  in  1895-96,  and  the  increase  in  car 
bonic  acid  may  be  considered  as  follows: 

PERCENTAGE  INCREASE  OF  CARBONIC  ACID 
(CARBON  DIOXIDE)  IN  THE  EFFLUENT 
ABOVE  THAT  IN  THE  RIVER  WATER. 

Maximum.     Minimum.     Averape. 

With  sulphate  of  alumina 41  9 

With  persulphate  of  iron 55 

Expressing  these  changes  in  actual  quanti 
ties,  the  following  comparisons  are  obtained: 

COMPARISON    OF    THE    MAXIMUM    AND    AVER 
AGE  AMOUNTS  OF  CARBON  DIOXIDE  IN  THE 
EFFLUENT  AND   IN   THE   RIVER  WATER. 
(Parts  per  Million.) 

Maximum.        Averagt. 

Ohio  River  water '33 

Effluent  with  sulphate  of  alumina 145 

Effluent  with  persulphate  of  iron 149 


WATER  PURIFICATION  AT  LOUISVILLE. 


At  this  point  it  is  to  be  stated  that  the  evi 
dence  obtained  in  1897  upon  the  corroding 
action  of  the  effluent  upon  iron  was  very  dif-  | 
ferent  (independent  of  the  influence  of  sus 
pended  matter),  and  much  more  favorable 
than  was  the  case  with  the  limited  data  in 
1890.  The  reasons  for  this  are  twofold. 

1.  In    1890  there  were  times  when  the  ap-   , 
plied  sulphate  of  alumina  for  considerable  pe 
riods  averaged  as  high  as  from  6  to  8  grains 
per  gallon;    while  in  1897  it  was  learned  that 
with  a  proper  use  of  subsidence  the  maximum 
limit  could  be  held  at  about  one-half  of  that 
stated  above. 

2.  The  limited  data  in   1896  indicated  that 
the  amount  of  free  carbonic  acid  in  the  Ohio 
River  water  ranged  from  20  to  30  parts  per 
million,  while  the  more  extended  series  of  op 
erations    in    1897    showed    that    the    amount 
reached  as  high  as   J  50  and  averaged  about 
70  parts.     Further,  the  later  results  showed 
that  it  was  very  seldom  that  the  amount  was 
less  than   50  parts,  clearly  proving  that  the 
amounts   found   when   in    1896   were   abnor 
mally  low  to  an  extreme  degree.      The  ex 
planation  of  this  is  not  entirely  known,   but 
it  was  partly  due  to  the  inaccuracies  of  Patten- 
kofer's  method  of  determining  carbonic  acid. 

From  these  and  other  facts  it  was  computed 
that  the  average  percentage  increase  in  car 
bonic  acid  was  about  40  per  cent,  under  the 
conditions  and  data  of  1896.  and  only  about 
9  per  cent,  for  1897.  Another  very  significant 
condition  which  obtained  from  time  to  time 
during  the  latter  part  of  the  tests  of  1896.  and 
which  was  absent  in  1897,  was  the  presence 
of  undecomposed  chemicals  in  the  effluent. 
This  was  of  great  importance  in  this  connec 
tion,  because  when  corrosion  is  once  started 
by  an  effluent  containing  sulphuric  acid,  the 
conditions  are  much  more  favorable  for  a 
continuance  of  the  action  by  carbonic  acid. 

As  has  been  stated  repeatedly,  the  presence 
of  undecomposed  chemicals  in  the  effluents  is 
inadmissible  for  many  reasons,  and  with 
proper  subsidence  facilities  its  occurrence 
would  be  inexcusable. 

The  carbonic  acid  liberated  by  the  decom 
position  of  carbonate  of  lime  is  the  same,  so 
far  as  its  corroding  nature  is  concerned,  as 
an  equal  amount  of  carbonic  acid  naturally 


present  in  the  water.  As  the  results  of  a 
large  number  of  experiments,  under  the  con 
ditions  indicated  to  be  most  suitable  for 
practical  purification,  it  was  found  that  the 
small  increase  in  carbonic  acid  produced  only 
very  slightly  greater  corroding  action  than 
possessed  by  the  river  water  after  removing 
the  suspended  matter  with  a  Pasteur  filter. 
In  fact  in  a  large  portion  of  the  tests  made  in 
bottles  with  rods  of  bright  wrought  iron  the 
increased  corrosion  was  not  appreciable. 

To  remove  the  small  amounts  of  carbonic 
acid  added  to  the  water  by  the  application  of 
sulphate  of  alumina  or  persulphate  of  iron, 
and  leave  the  large  amounts  naturally  and 
normally  present  in  the  river  water  would  be 
impracticable.  The  cost  of  chemical  per  mil 
lion  gallons  for  removing  i  part  per  million 
of  carbonic  acid,  with  lime  at  $3.75  per  ton, 
would  be  2.2  cents.  As  lime  is  only  sparingly 
soluble  in  water  it  would  be  necessary  to 
pump  daily  for  a  25-million-gallon  plant 
about  1750  gallons  of  water  in  order  to  pre 
pare  sufficient  lime-water  to  remove  t  part 
per  million  of  carbonic  acid. 

In  view  of  the  fact  that  corrosion  would  af 
fect  onlysuchiron  pipes  or  receptacles  as  were 
not  properly  coated  with  a  protective  paint, 
it  would  not  be  justifiable  to  remove  carbonic 
acid  to  a  point  where  it  would  not  possess  a 
corroding  action.  A  better  way  would  be  to 
protect  the  piping  system  as  it  is  extended  as 
far  as  possible  by  protective  paints,  and  to 
keep  the  quantities  of  applied  chemicals  as  low 
as  possible  by  taking  full  advantage  of  subsid 
ence.  With  regard  to  the  piping  system  al 
ready  in  service,  it  is  probable  that  such 
portions  as  are  not  already  protected  by  a 
coat  of  paint  are  protected  in  a  considerable 
measure  by  the  deposit  of  suspended  matter 
of  the  water  which  has  passed  through  them. 


Action  of  tlic  Effluent  on  Lead  Pipe. 

As  in  the  case  of  unpnrified  Ohio  River 
water,  the  effluent  would  contain  enough  car 
bonic  acid  and  carbonate  of  lime  to  form  very 
quickly  basic  carbonate  of  lead  which  is  in 
soluble  and  makes  an  impervious  protective 
coatino-. 


SUMMARY  AND  DISCUSSION  OF  DATA  OF  1807. 


435 


SKCTION  No.  15. 

COMPARATIVE  COSTS  OF  EQUIVALENT 
AMOUNTS  OF  THE  SEVERAL  AVAILABLE 
COAGULANTS,  TOGETHER  WITH  AN  ES 
TIMATE  OF  THE  YEARLY  COST  OF 
TREATMENT  OF  THE  OHIO  RIVER 
WATER  BY  EACH  OF  THEM. 

As  has  been  shown  in  the  preceding  sec 
tions  of  this  chapter,  the  coagulants  available 
for  use  in  the  purification  of  the  Ohio  River 
water  are  hydrate  of  alumina  prepared  by  the 
decomposition  of  sulphate  of  alumina  by  the 
lime  in  the  river  water,  hydrate  of  iron  pre 
pared  by  the  similar  decomposition  of  per 
sulphate  of  iron,  and  hydrate  of  iron  prepared 
by  the  electrolytical  decomposition  of  metal 
plates.  The  relative  advantages  and  disad 
vantages  of  each  have  been  presented  at  con 
siderable  length  both  in  absolute  and  com 
parative  terms,  and  it  remains  to  show  the 
exact  relative  and  annual  costs  of  these  three 
coagulants.  In  regard  to  the  sulphates,  this 
evidence  has  already  been  presented  in  a  gen 
eral  way,  but,  for  completeness,  they  will  be 
taken  up  again  here. 

Comparative  Cost  of  Equivalent  Amounts  of  the 
Available  Coagulants. 

In  section  Xo.  6  of  this  chapter  it  was 
shown  that  the  amounts  of  treatment  with 
persulphate  of  iron  and  with  electric  current 
on  iron  electrodes,  equivalent  to  i  grain  per 
gallon  of  sulphate  of  alumina  (containing  9.87 
per  cent,  of  aluminum)  were  as  follows:  Per 
sulphate  of  iron  (containing  24.43  per  cent, 
of  iron),  i  grain  per  gallon;  electric  current 
on  iron  electrodes.  0.04  ampere-hour  per 
gallon. 

In  regard  to  the  two  sulphates  the  com 
parison  of  cost  is  a.  simple  one.  but  in  regard 
to  the  electrolytically  prepared  coagulant 
there  are  several  separate  items  which  must 
be  taken  into  consideration. 

In  the  following  comparisons  no  account  is 
taken  of  cost  of  attendance,  which  would  be 
slightly  greater  in  the  case  of  the  electro 
lytic  treatment  than  in  the  case  of  the  sul 
phates.  The  cost  of  construction  of  devices 
for  the  application  of  the  sulphates  is  also  not 


considered  as  it  would  be  comparatively 
small  for  a  gravity  flow,  and,  owing  to  the 
limitation  in  the  amount  of  safe  electrolytic 
treatment,  these  devices  would  be  required 
in  the  use  of  any  of  the  coagulants. 

Cost  of  Electrolytic  Treatment  with  Iron  Elec 
trodes. 

In  the  cost  of  preparation  of  hydrate  of 
iron  by  the  action  of  an  electric  current  on 
iron  electrodes  the  following  items  must  be 
considered: 

1.  Cost  of  construction  of  electrolytic  cells. 

2.  Cost  of  construction  of  electrodes. 

3.  Cost    of    construction    of    electric    gen 
erating  appliances,  together  with  the  neces 
sary  building  to  cover  them. 

4.  Cost  of  operation  of  electric  appliances. 

5.  Cost  of  metal  used  in  the  formation  of 
the  hydrate  and  wasted  in  the  process. 

In  this  connection  it  is  considered  that  the 
Water  Company  owns  the  necessary  avail 
able  land  on  which  to  construct  the  buildings 
and  cells. 

For  the  several  items  the  following  esti 
mates  of  cost  are  used: 

i.  Cost  of  Construction  of  Electrolytic  Cells. 

As  will  be  seen  the  practical  size  of  the  nec 
essary  cells  would  be  so  great  that  open  chan 
nels  of  masonry  would  be,  apparently,  most 
suitable.  For  ease  of  handling  it  is  assumed 
that  plates  4  feet  wide,  3  feet  deep,  and  0.5 
inch  thick  would  be  employed  for  the  elec 
trodes.  It  is  further  assumed  that  a  o.5-inch 
length  of  electrolyte  (water  space  between 
the  plates)  would  be  most  advantageous. 

With  walls  and  bottom  i  foot  thick  the 
masonry  required  on  this  basis  would  be 
0.090  cubic  foot,  or  0.00334  cubic  yard  per 
square  foot  of  cross-section  of  electrolyte. 
At  $30.00  per  cubic  yard  the  cost  for  masonry 
would  therefore  be  $0.100  per  square  foot  of 
cross-section  of  electrolyte.  At  5  per  cent, 
interest  per  annum  this  would  represent  an 
expenditure  of  $0.0000137  per  day  (or  per 
twenty-five  million  gallons)  for  each  square 
foot  of  electrolyte,  or  $0.0137  per  1000  square 
feet  of  electrolyte. 


436 


WATER  PURIFICATION  AT  LOUISVILLE. 


In  the  following  computations  the  letters 
C.  S.  E.  will  be  used  to  represent  the  cross- 
section  of  electrolyte  in  thousands  of  square 
feet. 

2.  Cost  of  Construction  of  Electrodes. 

The  area  of  one  side  of  all  plates  would  cor 
respond  practically  to  the  area  of  cross-sec 
tion  of  electrolyte.  The  weight  of  metal  re 
quired  would  therefore  be  (on  the  above 
assumption  of  size  of  plates)  approximately 
20.0  pounds  per  square  foot  of  cross-section 
of  electrolyte,  and  would  cost  at  2  cents  per 
pound  (in  place)  40  cents.  The  daily  interest 
on  this  amount  would  be  $0.0554  x  C.S.E. 

j.  Cost  of  Construction  of  Electric  Generating 

Appliances,  together  with  the  Necessary 

Building  to  Cover  Them. 

From  preliminary  estimates  on  the  re 
quired  size  of  these  appliances  it  is  assumed* 
that  they  could  be  constructed  at  a  cost  of 
$170.00  per  indicated  H.P.,  or  allowing  one- 
third  for  a  reserve  plant,  $220.00  per  actual 
average  I.H.P.  The  interest  on  this  would  be 
$0.030  per  day,  per  I.H.P. 

4.  Cost  of  Operation  of  Electric  Generating  Ap 
pliances. 

It  is  assumed  that  a  combined  efficiency  of 
80  per  cent,  could  be  expected,  and  that  the 
consumption  of  coal  would  be  1.33  pounds 
per  I.H.P.  per  hour. 

The  required  amount  of  current  to  treat 
25  million  gallons  per  24  hours  with  0.04  am 
pere-hour  per  gallon  would  be  41,600  am 
peres. 

Using  the  average  resistance  of  the  electro 
lyte  as  presented  in  section  No.  3  of  this 
chapter,  7000  ohms  per  centimeter  cube  or 
9.65  ohms  per  sqdare  foot  of  cross-section  of 
electrolyte  with  a  o.5-inch  length  of  electro 
lyte  (water  space  between  plates),  the  re- 

17  900 
quired  amount  of  power  would  be 


C.S.E. 


The  daily  cost  would  be 


$571.00 


C.S.E. 


5.  Cost  of  Metal  Used  in  the  Formation  of  the 
Hydrate  and  Wasted  in  the  Process. 

As  was  shown  in  section  No.  4  of  this 
chapter,  the  total  amount  of  metal  used  in 
this  process  is  1.05  grams  per  ampere-hour. 
To  treat  25  million  gallons  with  0.04  ampere- 
hour  per  gallon  there  would  be  required 
therefore  2305  pounds  of  metal,  which  at 
2  cents  per  pound  would  cost  $46.10. 


Summary  of  Cost. 

The  several  items  may  now  be  summed  up 
as  follows: 

1.  Daily  interest  on  cost  of  construction  on 
electrolytic  cells,  $0.0137  x  C.S.E. 

2.  Daily  interest  on  cost  of  construction  of 
electrodes,  $0.0554  x  C.S.E. 

3.  Daily  interest  on  cost  of  construction  of 
electric    generating    appliances,    $0.030    per 

$537-°° 

[.II. P.,  or  -      — . 
C.S.E. 

4.  Daily  cost  of  generating  electric  power, 

$570.00 

$0.0319  per  I.H.P.  per  24  hours,  or  —      — . 

C.S.E. 

5.  Daily  cost  of  metal  used,  $46.10. 
Total  ($0.0137  +  $0.0554)  x  C.S.E. 

$537 +  $570 
+  —  —  +  $46.10. 

C.S.E. 

This  is  evidently  a  minimum  when  the 
values  of  the  two  variables  are  equal,  or  when 
the  cross-section  of  the  electrolyte  is  126,500 
square  feet. 

With  this  cross-section  the  potential  differ- 

8.65x41  600 
ence  between  the  plates  would  be —  — , 

126  500 
or  3.18  volts. 

The  cost  would  be  as  follows: 

1.  Electrolytic  cells,  422  cubic  yards 

masonry,  daily  interest. $T-73 

2.  Electrodes,  1265  tons  of  iron,  daily 

interest 7.00 

3.  Construction    of   generating   appli 

ances,  142  average  actual  indi 
cated  H.P.,  42  I.H.P.  reserve, 
daily  interest 3.90 


SUMMAKY  AND  DISCUSSION  OF  DATA    OF  1897. 


437 


4.  Operation     of     generating     appli 

ances,  142  average  I.H.P.,  daily 

cost 4.51 

5.  Metal  used  per  day 46. 10 


Total  cost $63.24 

Cost  of  Treatment  with  Persulphate  of  Iron. 

In  regard  to  the  sulphates  it  has  already 
been  show  that  their  value  is  dependent 
upon  the  amount  of  available  metal  which  they 
contain.  In  the  purchase  of  these  chemicals  it 
is  necessary,  therefore,  to  consider  their  com 
position.  The  persulphate  of  iron  which  was 
used  in  these  tests  contained  24.43  Per  cent, 
of  iron  and  was  of  approximately  equal  effi 
ciency  to  sulphate  of  alumina  containing  9.87 
per  cent,  of  aluminum.  It  is  stated  that  this 
chemical  could  be  purchased  in  carload  lots 
F.O.B.  cars,  Louisville,  for  $1.25  per  hun 
dred  pounds.  To  treat  25  million  gallons 
with  i  grain  per  gallon  would  cost,  therefore, 
$44.62. 

Cost  of  Treatment  with  Sulphate  of  Alumina. 

During  the  investigations  of  1897  three  dif 
ferent  lots  of  sulphate  of  alumina  were  em 
ployed.  These  lots  contained  different 
amounts  of  alumina  and  were  purchased  at 
different  prices  as  follows: 


Lot. 
A.. 
15  .  . 
C.. 


9.87 

8.46 

10.41 


1.50  cents 
1.40      " 
i.f'5      " 


As  the  value  of  a  coagulating  chemical  de 
pends  on  the  amount  of  hydrate  forming 
metal  which  it  contains,  the  costs  of  these 
three  lots  of  chemicals  must  be  reduced  to 
the  cost  per  pound  of  aluminum  in  order  to 
compare  them.  These  figures  are  as  follows: 

[  o(  Pounds  Aluminum  per  Cost  per  Pound 

I'ound  Sulphate.  Aluminum. 

A 0.0987  15.2  cents 

B 0.0846  16.5     ' 

C 0.1041  15.9     ' 


The  above  comparisons  illustrate  the  ne 
cessity  of  purchasing  these  chemicals  by  the 
amount  of  metal  which  they  contain.  In  the 
purchase  of  large  lots  it  would  undoubtedly 
be  best  to  receive  bids  based  on  the  amount 
of  available  aluminum  in  the  sulphate  offered. 
In  all  of  these  estimates  lot  A  is  used  as  a 
basis. 

The  cost  of  treating  25  million  gallons  of 
water  with  i  grain  per  gallon  of  lot  A  would 
be  $53-55- 

Summary. 

The  costs  of  treatment  of  25  million  gal 
lons  of  Ohio  River  water  with  the  equivalent 
of  i  grain  per  gallon  of  sulphate  of  alumina 
containing  9.87  per  cent,  of  aluminum,  by  the 
three  available  coagulants,  would  be  as  fol 
lows: 

Electrolytic  iron  treatment $63.24 

Persulphate  of  iron  44-62 

Sulphate  of  alumina   "         53-55 

Animal    Cost    of    Treatment    of    Twenty-five 
Million  Gallons  Daily  of  Ohio  River  Water. 

The  average  amounts  of  the  different  meth 
ods  of  treatment  which  would  be  required  to 
purify  the  Ohio  River  water  at  Louisville 
have  been  presented  in  section  No.  13  of  this 
chapter.  Combining  the  averages  given  there 
with  the  relative  cost  of  the  different  treat 
ments  as  given  above,  the  average  annual  cost 
of  treatment  by  the  three  methods  of  treat 
ment  is  obtained  as  follows: 

Estimated  Average  Annual  Cost  of  Treatment. 

Electrolytic  iron $40  400 

Persulphate  of  iron 28  500 

Sulphate  of  alumina 34  300 


438 


WATER   PURIFICATION  AT  LOUISVILLE. 


CHAPTER    XVI. 


FINAL  SUMMARY  AND  CONCLUSIONS. 


FOR  the  sake  of  convenience  and  explicit- 
ness,  the  leading  points  of  practical  signifi 
cance  are  brought  together  in  brief  terms  in 
this  chapter.  The  circumstances  under  which 
the  investigations  and  tests  were  conducted 
caused  the  evidence  upon  many  of  the  points 
to  appear  in  several  chapters;  but  with  the 
aid  of  the  accompanying  index  detailed  in 
formation  upon  the  important  features  of  the 
work  may  be  obtained  readily. 

Character  of  the  Unpurified  Ohio  River  Water. 

The  suspended  mud,  silt,  and  clay  in  the 
Ohio  River  water  make  it  in  many  respects 
an  undesirable  water  for  a  municipal  supply, 
and  the  large  amounts  and  wide  variations  in 
the  size  and  character  of  the  suspended  mat 
ter  make  it  a  difficult  and  expensive  water  to 
purify.  With  regard  to  the  sanitary  character 
of  the  river  water,  the  large  amounts,  during 
the  greater  portion  of  the  year,  of  suspended 
organic  and  mineral  matter  cannot  be  con 
sidered  other  than  as  objectionable,  although 
there  is  no  evidence  to  lead  to  the  belief  that 
these  matters  exert  a  specifically  injurious 
effect  upon  persons  in  normal  health.  In  fact 
it  is  in  the  low  stages  of  the  river  when  the 
water  is  comparatively  clear  that  its  hygienic 
character  is  least  satisfactory.  During  the  fall 
months  there  were  repeatedly  noted  unmis 
takable  signs  of  contamination  of  this  water 
supply  by  the  sewage  of  the  cities  located 
above  it;  and  from  time  to  time  throughout 
the  year,  the  conditions  manifested  them 
selves  in  the  presence  in  the  water  of  bacillus 
coli  communis,  which  is  the  most  prevalent 
germ  in  the  feces  of  man  and  certain  domes 
tic  animals.  The  result  of  all  tests  for  specific 
germs  of  disease,  however,  were  negative. 

Practically    speaking,    the    significance    of 


this  is  that  when  the  river  is  high  and  the 
water  muddy  the  water  is  not  dangerous,  al 
though  it  is  not  free  of  suspicion  for  drinking 
purposes.  When  the  river  is  low  and  the 
water  clear,  however,  the  healthfulness  of  the 
water  is  always  questionable,  and  the  degree 
of  danger  which  its  use  involves  depends 
upon  the  prevalence  of  disease  in  the  cities 
higher  up  in  the  valley.  If  an  epidemic  of 
cholera  or  typhoid  fever  should  break  out  in 
any  of  the  upper  cities,  there  are  at  present  no 
reliable  means  of  preventing  the  specific 
germs  of  disease  from  passing  in  more  or  less 
diminished  numbers  from  the  outfall  sewers 
of  the  upper  city  by  the  river,  to  and  through 
the  reservoir  and  distributing  mains,  to  the 
service  pipes  of  the  water  consumers  at  Louis 
ville.  It  is  true  that  several  natural  agencies 
such  as  dilution  and  sedimentation  in  the  river 
and  reservoir  tend  to  remove  these  germs  in 
a  large  measure,  but  such  means  cannot  be 
depended  upon  now.  As  the  population  on 
the  watershed  increases,  with  no  correspond 
ing  and  compensating  changes  in  the  natural 
conditions  causing  the  removal  from  the 
water  of  sewage  germs,  the  healthfulness  of 
the  river  water  will  continue  to  decrease 
steadily  and  surely.  Under  these  conditions 
it  is  imperative  that  whatever  method  of  puri 
fication  be  adopted,  it  shall  be  capable  of  pro 
tecting  the  water  consumers  from  water- 
borne  diseases,  because  if  this  were  not  done 
the  expenditure  of  the  large  sums  of  money 
necessarily  involved  in  purification  would  not 
be  justifiable. 

With  regard  to  the  storage  and  distribu 
tion  of  the  unpurified  Ohio  River  water,  the 
amount  of  suspended  matter  in  the  water  pre 
vents  the  penetration  of  the  rays  of  the  sun, 
when  stored  in  an  open  reservoir,  to  such  a 
degree  that  under  ordinary  circumstances  no 


FINAL  SUMMARY  AND  CONCLUSIONS. 


43'J 


growths  occur  of  algse,  etc.,  which  give  rise  to 
the  objectionable  tastes  and  odors.  The  water 
contains  an  ample  supply,  however,  of  soluble 
mineral  matter  suitable  as  a  food  for  the  mi 
cro-organisms.  Carbonic  and  oxygen  gases 
are  dissolved  in  the  water  in  such  amounts 
that  the  water  has  considerable  corroding  ac 
tion  upon  iron  pipes  which  are  not  coated 
with  a  protective  paint.  This  corroding  ac 
tion  is  much  retarded  by  the  suspended  mat 
ters  of  the  water,  as  they  serve  in  a  measure 
in  forming  protective  coatings.  The  Ohio 
River  water  under  the  conditions  met  with 
in  practice  has  no  objectionable  action  on 
lead  pipes,  because  the  water  quickly  forms 
insoluble  basic  carbonate  of  lead  which  gives 
to  the  pipe  an  impervious  protective  coating. 
For  use  in  steam-boilers  the  Ohio  River 
water  is  not  very  desirable  when  compared 
with  the  soft  and  clear  waters  of  the  East. 
Nevertheless,  comparing  it  with  the  still 
harder  waters  met  with  farther  West,  it  is 
fairly  satisfactory  for  boiler  use.  When  the 
river  water  is  muddy  it  forms  in  boilers  large 
amounts  of  sludge  which  are  removed  with 
much  difficulty  on  some  occasions,  as  this 
sludge  cannot  be  "  blown  off."  At  such 
times  the  amounts  of  sulphate  of  lime  and  of 
other  incrusting  constituents  are  small  and 
they  arc  deposited  upon  the  sludge  for  the 
most  part  and  not  upon  the  metal  of  the  boil 
ers.  During  the  fall  months,  however,  when 
the  river  water  is  fairly  clear  the  amounts  of 
incrusting  constituents  are  much  larger  than 
usual,  and  the  fine  clay  in  the  water  at  such 
times  unites  with  the  sulphate  of  lime,  etc..  to 
form  a  scale  resembling  cement  and  which  is 
very  difficult  to  remove. 

Applicability   to    the    Purification    of   the    Oliio 
River  Water  of  the  Three  Methods  Investi 
gated  during  these  Tests. 

Three  methods  of  purification  were  tested 
with  general  results  as  follows: 

i.  The  general  method  embodying  subsi 
dence  (sedimentation),  coagulation,  and  fi1- 
tration,  such  as  was  practiced  in  part  in  the 
Warren.  Jewell,  and  two  Western  systems,  is 
correct  in  principle  for  the  practicable  purifi 
cation  of  this  water.  Tt  had  several  weak 
nesses,  as  practiced  in  these  tests,  the  most 


important  one  being  the  totally  inadequate 
facilities  in  all  cases  for  the  employment  of 
subsidence  to  its  proper  economical  limits. 
This  is  shown  more  clearly  beyond. 

_'.  The  I  larris  Magneto-Electric  System 
was  a  complete  failure. 

3.  The  MacDougall  Polarite  System  as  it 
was  tested  by  this  Company  was  not  ap 
plicable  to  the  purification  of  the  ( )hio  River 
water. 

Imperativeness  of  the  Use  of  Coagulants. 

Owing  to  the  fact  that  at  times  this  river 
water  contains  large  amounts  of  very  minute 
clay  particles  (many  of  which  are  as  small  as 
o.ooooi  inch  in  diameter),  it  may  be  stated  in 
unqualified  terms  that  at  least  for  several  suc 
cessive  weeks  in  the  spring  and  early  summer, 
successful  and  economical  purification  of  this 
water  makes  the  use  of  coagulation  impera 
tive  in  connection  with  subsidence. 

Whether  or  not  it  is  absolutely  essential  or 
desirable  to  employ  coagulation  in  connec 
tion  with  filtration  of  a  properly  subsided 
water  is  a  problem  which  would  depend  upon 
the  rate  of  filtration,  but  upon  which  no 
specific  data  were  obtained  in  these  tests. 

Relative  Applicability  of  American  anil  English 
Types  of  filters. 

With  regard  to  the  filtration  of  the  Ohio 
River  water  after  partial  purification  by  plain 
subsidence  and  subsidence  aided  at  times  by 
coagulation,  by  the  American  and  English 
types  of  filters,  no  comparisons  were  made 
during  these  investigations.  Taking  into 
consideration,  however,  the  general  informa 
tion  obtained  in  these  tests  as  to  the  character 
of  the  water,  combined  with  the  results  of  the 
tests  made  with  English  filters  in  1884.  the 
indications  point  to  the  superiority  of  the 
American  filters  for  this  water,  owing  to  their 
improved  facilities  for  cleansing  the  sand 
layer.  Here  it  may  be  noted  that  the  tests  in 
1884-85  were  made  for  about  eight  months 
in  tanks  12  feet  in  diameter.  The  water  pass 
ing  on  to  the  filter  was  subsided  for  about  six 
days  in  the  Crescent  Hill  reservoir  without 
coagulants.  During  this  period  the  excessive 
amounts  of  fine  clay,  as  found  frequently  in 
the  spring,  were  largely  absent.  The  filters 
were  constructed  after  the  English  plan,  as 


440 


WATER  PURIFICATION  AT  LOUISVILLE. 


recommended   and   described   by   Kirkwoocl, 

and  the  sand  had  an  effective  size  of  0.36 
millimeter.  This  agrees  very  closely  with 
the  sixe  of  sand  employed  in  the  best  filters 
in  Kurope. 

As  a  result  of  the  tests  of  1884-85  it  was 
learned  that  the  clay  could  be  removed  and 
an  effluent  free  of  turbidity  secured  by  Eng 
lish  filters  at  a  net  rate  of  about  1.5  million 
gallons  per  acre  daily,  lint  the  principal 
point  of  practical  significance  was  the  marked 
indication  of  the  clay  passing  into  the  sand 
layer,  and  the  necessity  of  cleaning  and  recon 
structing  the  sand  layer  at  periods  of  com 
paratively  short  duration. 

Removal  of  Coarse  Mailers  by  Plain 
Subsidence. 

The  entire  absence  of  this  very  important 
and  essential  feature  of  successful  purification 
of  water  of  this  character  comprised  the 
greatest  weakness  of  all  the  systems  tested. 
This  subject  was  given  considerable  attention 
on  a  laboratory  scale,  and  it  was  found  that 
with  ordinary  muddy  water  about  24  hours 
of  quiescent  subsidence  in  one-gallon  bottles 
caused  a  removal  of  about  75  per  cent,  of  the 
suspended  matters  by  weight.  As  it  is  well 
known  that  on  a  large  scale  the  quiescent 
state  of  the  water  cannot  be  obtained  in  so 
short  a  time,  the  above  period  is  only  of  pass 
ing  significance  in  connection  with  laboratory 
experiments,  and  for  the  most  practicable 
conditions  on  a  large  scale  it  is  necessary  to 
rely  upon  information  from  other  sources. 
This  subject  is  dealt  with  in  section  No.  T  of 
Chapter  XV,  and  it  may  be  added  that  in 
practice  the  period  should,  in  all  probability, 
be  much  longer  than  24  hours. 

Most   Suitable   Coagulant   for   the   Ohio   River 
Water. 

All  things  taken  into  consideration,  the 
most  suitable  coagulant  at  present  for  the 
treatment  of  the  Ohio  River  water  is  sulphate 
of  alumina.  Persulphate  of  iron  in  equiva 
lent  amounts  is  now  slightly  cheaper,  but  the 
difference  is  not  sufficient  to  offset  certain 
advantages  of  sulphate  of  alumina. 

The  electrolytic  production  of  aluminum 
hydrate  from  metallic  aluminum  electrodes  is 


impracticable,  both  on  the  grounds  of  ex 
cessive  cost  and  of  irregularities  in  efficiency. 
With  regard  to  the  electrolytic  production  of 
iron  hydrate  from  iron  electrodes  this  process 
yields  a  satisfactory  coagulant  up  to  the 
equivalent  of  3  grains  per  gallon  of  sulphate 
of  alumina.  Beyond  this  point  it  could  not 
be  safely  employed  in  midsummer,  when  the 
amount  of  dissolved  oxygen  in  the  water  is 
inadequate  to  oxidize  larger  quantities. 
Combining  the  cost,  the  limitations  in  the 
amount  which  can  be  safely  applied  without 
the  presence  of  iron  in  the  effluent  and  cer 
tain  irregularities  upon  reversing  the  direc 
tion  of  the  electric  current,  this  process  is  not 
considered  advisable. 

Concerning  the  Anderson  process  for  the 
preparation  of  iron  hydrate  directly  from 
metallic  iron,  the  results  of  laboratory  tests 
indicate  that  it  is  not  applicable  for  the  eco 
nomic  and  efficient  purification  of  the  Ohio 
River  water. 

Of  the  various  chemicals  mentioned  in 
section  No.  2  of  Chapter  XV,  no  others  were 
found  practicable. 


The  method  of  dissolving  known  amounts 
of  the  chemical  in  known  volumes  of  water 
is  the  best. 

The  passage  of  a  stream  of  water  through 
a  cylinder  containing  the  chemical  is  not 
practicable. 

Concerning  the  application  of  the  solutions 
of  the  chemical  the  Warren  device  was  fairly 
automatic,  but  possessed  several  faults,  the 
chief  one  of  which  was  the  failure  in  the  op 
eration  of  the  device  when  the  flow  of  water 
fell  below  a  certain  quantity.  The  pumps 
used  in  the  Jewell  and  modified  Western 
systems  were  satisfactory,  but  required  great 
care  and  close  attention. 

Taking  everything  into  consideration  it  is 
believed  that  in  practice  the  discharge  of  a 
solution  by  gravity  would  be  the  most  ad 
visable. 

Coagulation  and  Subsidence. 
In  addition  to  plain  subsidence  and  to  co- 


FINAL    SUMMARY  AND   CONCLUSIONS. 


441 


agulation  given  to  water  just  prior  to  filtra 
tion,  there  are  times  when  coagulation  in  con 
junction  with  subsidence  can  be  employed  to 
advantage  in  keeping  clay  and  other  sus 
pended  matters  from  passing  on  to  the  sand 
layer.  Such  times  would  occur  in  practice 
when  the  water  after  plain  subsidence  would 
require  more  than  from  1.5  to  2.0  grains  per 
gallon  of  sulphate  of  alumina  for  thorough 
coagulation.  In  this  respect  all  of  the  sys 
tems  were  lacking,  although  the  practical  sig 
nificance  of  this  point  was  realized  by  the 
operators  of  the  Warren  System,  as  shown  by 
their  division  of  the  application  of  coagulants 
in  July,  1896. 

With  regard  to  the  optimum  period  of  time 
to  provide  for  the  accomplishment  of  coagu 
lation  and  subsidence,  it  would  vary  accord 
ing  to  the  amount  and  character  of  the  sus 
pended  matters  present  in  the  water  after 
plain  subsidence  had  taken  place.  The  indi 
cations  are  that  it  might  reach  or  exceed 
6  hours  in  many  instances,  but  the  economic 
period  would  be  limited  by  the  cost  of  sub 
siding  facilities. 

Coagulation  and  Filtration. 

After  the  river  water  has  been  properly 
treated  by  subsidence  for  the  removal  of  sus 
pended  matters,  it  is  imperative  that  the  water 
as  it  reaches  the  sand  layer  be  thoroughly 
coagulated  from  a  practical  point  of  view. 
In  the  absence  of  complete  coagulation,  or 
very  nearly  complete,  the  efficiency  of  nitra 
tion  cannot  be  uniformly  depended  upon. 

Concerning 'the  optimum  period  of  coagu 
lation  of  the  water  prior  to  nitration,  it  would 
vary  widely  from  time  to  time  in  the  purifica 
tion  of  this  water.  When  the  water  contains 
very  little  suspended  matter  the  period  should 
probably  be  not  more  than  half  an  hour.  But 
as  the  quantity  of  suspended  matter  increases, 
the  period  of  coagulation  (and  supplementary 
subsidence)  should  increase.  In  some  cases 
the  optimum  period  would  be  at  least  3  hours, 
and  probably  longer.  The  longest  period  of 
course  would  be  found  when  the  amount  of 
coagulant  fell  just  below  the  point  where 
economy  demands  a  division  in  the  applica 
tion  (1.50  to  2.00  grains  per  gallon). 


Point  of  Application  of  Coagulant  with  Refer 
ence  to  the  Period  of  Time  Elapsing  be 
tween  Application  and  the  Entrance  of  the 
Water  into  the  Sand  Layer. 

The  results  of  these  investigations  prove 
conclusively  that  at  the  present  time  no  fixed 
point  of  application  of  coagulant  would  fulfill 
the  demands  of  economy.  In  the  light  of  our 
present  knowledge,  the  devices  for  the  appli 
cation  of  coagulant  should  be  made  adjust 
able  with  reference  to  the  point  of  applica 
tion.  Whether  or  not  it  would  ever  be 
practicable  in  the  treatment  of  this  water  to 
confine  the  application  of  coagulants  to  a 
range  of  three  or  four  points  can  be  told  only 
by  experience  under  the  conditions  of  suc 
cessful  practice. 

Total  Annual  Average  Amounts  of  Sulphate 
of  Alumina  Required  for  Coagulation. 

Taking  into  consideration  the  fact  that  two 
periods  of  extended  droughts  occurred  dur 
ing  the  tests  of  1895-96,  the  data  show 
that  with  the  systems  tested  at  that  time  the 
annual  average  amounts  of  sulphate  of  alu 
mina  would  range  from  2.5  to  3.5,  and  aver 
age  about  3.0  grains  per  gallon  of  filtered 
water. 

By  taking  advantage  of  subsidence  to  its 
economical  limit,  the  investigations  of  1897 
indicate  clearly  that  this  could  be  held  at  from 
1.5  to  2.0  grains,  with  an  annual  average  of 
about  1.75  grains. 

In  these  comparisons  it  is  assumed  that  in 
each  case  a  good  grade  of  sulphate  of  alumina 
would  be  used. 

Filtration. 

In  respect  to  filtration  proper,  independent 
of  subsidence  and  coagulation,  the  Jewell  fil 
ter  on  the  whole  was  found  to  be  more  satis 
factory  than  the  others  examined  in  these 
tests. 

The  capacity  of  niters  of  this  type  is  con 
sidered  to  be  100  million  gallons  of  filtered 
water  per  acre  daily.  This  means  that  to  ob 
tain  one  million  gallons  of  filtered  water  in  24 
hours  it  would  be  necessary  to  provide  435.6 
square  feet  of  filtering  surface.  To  rate  these 
filters  at  a  lower  capacity  is  out  of  question, 


442 


WATER  PURIFICATION  AT  LOUISVILLE. 


and  the  indications  are  that  when  the  bulk  of 
the  suspended  matters  is  removed  by  sub 
sidence,  and  the  operation  of  a  system  placed 
on  a  practical  basis,  this  capacity  could  be 
safely  increased  to  meet  the  increased  con 
sumption  of  water.  It  is  probable  that  this 
capacity  under  the  stated  conditions  could  be 
raised  50  per  cent,  with  satisfactory  results. 

The  Jewell  filter  did  not  contain  all  01  the 
best  features  of  filters  of  this  type,  especially 
when  compared  with  the  Warren  filter,  and  it 
could  be  improved  in  a  number  of  ways,  both 
with  regard  to  construction  and  operation. 
An  outline  of  the  more  important  features 
which  successful  filters  in  practice  should 
comprise  is  as  follows: 

Essential  Features  of  American  Filters  for  the 

Successful  Filtration  of  Twenty-five  Million 

Gallons  of  Ohio  River  Water  Dail\. 

Experience  obtained  during  these  investi 
gations  shows  the  practical  importance  of  the 
following  points: 

Condition  of  the  Water  Entering  the  Sand 
Layer. — The  evidence  is  very  decisive  that  so 
far  as  practicable  the  suspended  matters 
should  be  removed  before  reaching  the  sand 
layer,  and  that,  at  that  point, the  water  should 
be  thoroughly  coagulated.  Further,  it  is 
clear  that  subsidence  should  be  employed 
with  waters  of  this  character  to  a  degree 
where  the  amount  of  coagulant  to  be  applied 
at  or  just  before  the  entrance  to  the  filter 
should  not  frequently  exceed  2  grains  per 
gallon. 

Failure  to  make  suitable  provisions  in  this 
respect  caused  the  Western  gravity  filter  to 
be  voluntarily  withdrawn  from  the  tests  be 
cause  it  was  unable  to  purify  enough  water, 
when  the  river  water  was  very  muddy,  to 
wash  its  own  sand  layer;  and  in  the  two  best 
niters,  the  Warren  and  Jewell,  it  may  be  con 
servatively  stated  that  to  maintain  the  full 
supply  at  times  of  heavy  freshets  it  would 
be  necessary  to  provide  reserve  filters  equa1 
to  75  per  cent,  of  the  normal  capacity  of  the 
plant.  Furthermore,  the  failure  in  these  sys 
tems  to  remove  the  coarser  particles  by  sub 
sidence  would  in  practice  cause  a  large  waste 
of  coagulants,  as  stated  above. 

Structure   of  Filters.  —  For   a   permanent 


plant  the  use  of  metal,  as  in  the  case  of  the 
Western  pressure  filter,  would  be  preferable 
to  wood.  The  foul  odors  in  the  bottom  of  the 
Warren  filter  when  it  was  removed  at  the 
ciose  of  the  tests,  shows  an  objection  to  the 
use  of  wood  for  closed  compartments. 

Size  of  Filters. — The  several  filters  repre 
sent  the  prevailing  size  in  practice,  but  tor 
economy  in  operation  the  individual  filters 
should  be  made  much  larger,  the  limit  to  be 
determined  by  the  successful  operation  of  me 
chanical  appliances  to  stir  the  sand  layer 
effectively  while  it  is  being  washed  by  a  re 
verse  flow  of  water. 

Location  of  Sand  Layers. — The  location  of 
the  sand  layer  near  the  top  of  the  filter  tank, 
as  in  the  case  of  the  Jewell  filter,  is  an  advan 
tage,  because  it  guards  against  the  waste  of 
coagulated  water  above  the  sand  layer  just 
prior  to  washing  and  it  would  also  reduce  the 
cost  of  construction. 

Character  of  Sand  Layers. — Experience  in 
dicates  that  in  all  cases  the  frictional  resist 
ance  to  the  flow  of  water  was  too  small.  This 
could  be  remedied  by  using  a  sand  of  finer 
grain  or  a  layer  of  greater  thickness,  or  both. 
In  the  judgment  of  the  writer  it  would  be  ad 
visable  to  maintain  a  thickness  of  30  inches 
and  employ  a  sand  having  an  effective  size  of 
0.35  millimeter.  This  would  increase  the 
frictional  resistance  of  the  sand  layer  in  the 
Jewell  filter  about  50  per  cent.,  other  condi 
tions  being  equal. 

Filtered  Water  E.rits. — The  Western  filter 
did  not  satisfactorily  meet  this  difficult  prob 
lem,  as  the  sand  passed  into  the  slotted 
brass  tubes.  In  the  Warren  filter  there  was 
little  chance  for  lateral  and  irregular  flow  of 
water  at  the  bottom  of  the  sand  layer,  except 
as  caused  by  the  supports  beneath  the  per 
forated  plate.  All  things  considered,  it  is  be 
lieved  that  the  Jewell  filter  was  superior  in 
this  respect,  although  it  would  probably  be 
advisable  to  double  the  number  of  strainer 
cups. 

Amount  and  Nature  of  Pressure  (Head). — 
The  indications  are  that  10  feet  for  a  maxi 
mum  acting  head  would  be  advisable  under 
the  conditions  of  practice.  So  far  as  could 
be  learned  the  negative  head  (suction)  in  the 
Jewell  filter  gave  directly  no  advantages  over 
a  positive  head  with  regard  to  the  efficiency 


FINAL  SUMMARY  AND  CONCLUSIONS. 


443 


of  the  filter.  In  consequence  of  a  negative 
head,  however,  there  are  several  advantages 
as  noted  above  in  connection  with  the  waste 
of  coagulated  water  and  the  cost  of  construc 
tion. 

There  were  no  indications  that  the  use  of  a 
pressure  filter,  as  represented  in  the  Western 
pressure  filter,  would  be  advisable  in  purify 
ing  this  water  supply. 

Rate  of  Filtration. — The  evidence  and  con 
clusions  upon  this  point  are  presented  above 
in  reference  to  the  capacity  of  filters. 

]V  ashing  the  Sand  Layer.  —  Experience 
showed  that  when  the  sand  layer  requires 
washing  it  should  be  done  thoroughly  with 
filtered  water,  and  that  accompanying  agita 
tion  of  the  sand  layer  is  an  advantage.  The 
agitator  of  the  Jewell  filter  was  of  a  type  su 
perior  to  that  in  the  Warren  filter,  but  the 
teeth  of  the  rake  arms  should  penetrate  as 
nearly  to  the  bottom  of  the  sand  layer  as 
safety  would  allow. 

Surface  Agitation. — This  process  could  be 
profitably  employed  to  a  greater  degree  in 
practice  than  was  the  case  in  the  Jewell  filter, 
the  only  one  of  these  filters  in  which  advan 
tage  of  this  was  taken  at  all.  In  practice  the 
filter  tank  should  be  designed  so  as  to  allow 
the  water  above  the  sand,  together  with  the 
surface  accumulations,  to  be  flushed  off  into 
the  sewer  during  agitation.  The  use  of  a 
finer  sand  would  also  be  an  advantage  in  this 
connection. 

•Application  of  Caustic  Soda. — From  time  to 
time  the  use  of  caustic  soda,  to  keep  the  sand 
free  of  matters  which  are  absorbed  and  at 
tached  to  it,  is  advisable. 

Attention. — This  is  a  very  important  factor 
in  the  efficiency  of  filters  of  this  type  in  the 
purification  of  the  Ohio  River  water,  and 
economy  as  well  as  efficiency  demands  that 
they  shall  receive  skilled  attention,  especially 
to  prevent  a  waste  of  coagulants.  With  suit 
able  provisions  for  subsidence,  the  necessary 
amount  of  care  and  skill  would  be  much  less 
than  indicated  by  these  tests,  after  the  plant 
had  been  placed  upon  a  practical  and  sys 
tematic  basis  of  operation. 

Accessibility  of  Parts. — Improvements  in  all 
of  these  filters  should  be  made  with  regard  to 
accessibility  of  parts,  in  order  to  facilitate  ex 
amination  and  repairs  whenever  necessary. 


Quality  of  the  Ohio  River  Water  after  Puri 
fication  by  Coagulation  and  Filtration,  pre 
ceded  by  Subsidence  so  far  as  Practi 
cable. 

With  proper  attention  to  the  operation  of 
a  system  as  outlined  above,  and  an  adequate 
degree  of  coagulation  (by  sulphate  of  alu 
mina)  of  the  water  as  it  enters  the  sand  layer, 
this  method  could  produce  a  quality  of  filtered 
water  which  would  be  thoroughly  satisfactory 
under  all  ordinary  conditions  with  regard  to 
appearance  and  sanitary  character. 

Owing  to  the  inherent  character  of  the 
Ohio  River  water  and  the  local  conditions, 
the  filtered  water  could  not  be  stored  in  open 
reservoirs,  except  for  very  short  periods,  with 
any  reasonable  assurance  that  algri1,  etc., 
coming  from  the  air  would  not  grow  in  the 
presence  of  sunlight  and  give  to  the  water 
objectionable  odors  and  tastes.  To  guard 
against  this  effectively  the  reservoir  in  which 
the  filtered  water  is  stored  should  be  covered. 

The  filtered  water  would  not  give  any 
trouble  in  the  case  of  lead  pipes,  or  in  iron 
pipes  which  are  properly  coated  with  pro 
tective  paints.  In  uncoated  iron  vessels  the 
corrosive  action  would  be  somewhat  greater 
than  in  the  case  of  river  water,  owing  princi 
pally  to  the  removal  of  suspended  matters, 
which  in  a  measure  act  as  a  protective  coating. 
With  regard  to  use  in  steam-boilers  there 
would  be  more  incrusting  constituents  than 
in  the  river  water,  although  the  annual  aver 
age  amount  in  the  filtered  water  would  be 
only  about  60  per  cent,  of  the  quantity  nor 
mally  present  in  the  river  water  during  the 
fall  months.  The  effect  of  this  addition  would 
be  largely  if  not  wholly  offset  by  the  removal 
of  the  suspended  matters;  and,  compared 
with  the  waters  of  other  cities,  it  \\ould  be 
classed  as  a  satisfactory  boiler  water. 

Final  Conclusion. 

The  general  method  of  subsidence,  coagu 
lation,  and  filtration  is  applicable  to  the  satis 
factory  purification  of  the  Ohio  River  water 
at  Louisville;  but, as  practiced  by  the  Warren, 
Jewell,  and  Western  systems  during  these 
tests,  its  practicability  is  very  questionable  if 
not  inadmissible.  By  removing  the  bulk  of 


444 


WATER   PURIFICATION  AT  LOUISVILLE. 


the  suspended  matters  from  the  water,  large 
reductions  could  be  made  in  the  size  of  filter 
plant,  amount  of  coagulant,  and  cost  of  op 
eration.  On  the  basis  of  twenty-five  million 
gallons  daily,  these  reductions  when  capital 
ized  at  5  per  cent,  would  represent  about 
$700,000.  There  is  no  room  for  doubt  but 
that  for  a  less  sum  than  this  satisfactory  pro 
visions  for  subsidence  as  outlined  herein 


could  be  provided,  which  would  not  only  aid 
in  furnishing  a  filtered  water  of  better  quality, 
but  would  also  give  the  water  consumers  a 
better  service  in  other  regards. 

Very  respectfully  submitted, 

GEORGE  W.  FULLER, 
Chief  Chemist  and  Bacteriologist. 
LOUISVILLE,  Kv.,  Oct.  7,  1897. 


APPENDIX. 


THE  appendix  consists  of  a  brief  technical 
resume  of  the  methods  of  analysis  which  were 
employed  during  these  tests  and  investiga 
tions,  together  with  some  notes  on  the  collec 
tion  of  samples. 

COLLECTION  OF  SAMPLES. 

The  only  departure  from  the  standard 
methods  and  technique  of  collection  of  sam 
ples  was  in  the  use  of  a  device  termed  the 
"  automatic  sampler." 

Automatic  Sampler. — For  the  purpose  of 
collecting  samples  which  should  be  represen 
tative  of  the  effluent  for  long  periods  of  time, 
the  device  described  below  was  arranged  and 
used  during  March,  April,  and  early  part  of 
May.  1896,  for  the  collection  of  samples  from 
all  the  systems,  and  from  May  n  to  July  23, 
1896,  for  the  collection  of  samples  for  chem 
ical  analysis  from  the  Western  Pressure  Sys 
tem.  The  device  consisted  of  a  brass  cylinder 
(A)  closed  at  one  end.  of  about  5  cubic  centi 
meters  capacity,  and  with  a  single  orifice  on 
one  side.  This  cylinder  was  ground  into  a 
covering  cylinder  (B)  in  which  it  was  revolved 
by  a  feathering  paddle-wheel  in  the  main  efflu 
ent  pipe.  The  wheel  was  operated  by  the  cur 
rent  and  was  designed  to  turn  at  a  rate  pro 
portional  to  the  flow  of  water  through  the 
pipe.  A  small  pipe  led  from  the  opposite  side 
of  B  to  the  collecting  bottle.  The  openings 
for  these  pipes  and  for  the  orifice  in  A  were 
in  the  same  plane.  An  air  pipe  with  protected 
end  was  provided  from  cylinder  A,  as  was 
also  an  escape  from  the  collecting  bottle.  The 
operation  was  as  follows:  As  cylinder  A  re 
volved  its  orifice  connected  with  the  inlet  ori 
fice  through  cylinder  B  and  water  from  trie 
effluent  pipe  entered  and  filled  cylinder  A 
and  the  air  tube.  As  cylinder  A  turned,  it 


cut  off  the  connection  with  the  inlet  pipe,  and 
when  one-half  around,  connected  with  the 
outlet  orifice  through  cylinder  B  and  the 
contents  of  the  cylinder  and  air  tube  were  dis 
charged  through  the  outlet  tube  into  the  col 
lecting  bottle.  In  this  manner  a  small  sample 
was  taken  at  each  revolution,  the  gearing- 
being  so  proportioned  that  at  the  normal  rate 
of  23.5  cubic  feet  per  minute,  about  six  sam 
ples  were  taken  each  minute.  A  gallon  bottle 
was  used  as  a  collecting  bottle.  The  whole 
device  was  inclosed  in  a  wooden  box. 

.    REGULAR  CHEMICAL  ANALYSES. 
Form  of  Expression. 

The  results  of.  the  determinations  of  the 
several  chemical  constituents  arc  expressed  in 
this  report  in  parts  by  weight  per  million 
parts  of  water  by  volume.  This  form  was 
adopted  mainly  for  the  reason  that  the  re 
sults  of  a  previous  series  of  analyses  for  this 
Company  had  been  expressed  in  this  manner. 

Turbidity. 

During  the  early  part  of  these  tests,  use  was 
made  of  the  adjectives  commonly  employed 
in  describing  the  results  of  inspection  of  the 
samples  as  they  appeared  after  settling  over 
night  in  one-gallon  bottles.  During  1896  a 
"  diaphanometer  "  was  used  for  a  time.  This 
instrument  consisted  of  a  brass  tube  in  which 
the  sample  of;  water  was  placed  and  through 
which  light  was  reflected  from  a  Welsbach  gas 
lamp.  The  turbidity  of  the waterwas  estimated 
as  the  reciprocal  of  the  length  of  a  column  of 
water  which  would  cause  the  image  of  a  cross 
of  black  lines  at  the  bottom  of  the  tube  to  dis 
appear.  Fairly  satisfactory  results  were  ob- 

445 


446 


APPENDIX. 


tained  with  waters  of  a  slight  but  noticeable 
turbidity;  but  it  appeared  to  be  inadequate 
for  regular  use  in  this  connection  with  satis 
factory  results  upon  the  fairly  clear  effluents 
or  verv  muchly  river  water. 


The  relative  amounts  of  sediment  in  the 
river  water  were  estimated  in  the  early  part  of 
the  work  by  inspection  of  the  samples  after 
settling  over  night  in  one-gallon  bottles. 
These  observations  seemed  to  be  of  but  little 
value,  and  later  were  abandoned,  comparison 
of  sediment  then  being  made  upon  the  parts 
by  weight  of  suspended  matter. 

Odor. 

The  odor  of  the  water  at  room  temperature 
and  after  heating  in  a  beaker  to  100°  C.  was 
observed  and  recorded,  respectively,  as  the 
"  cold  "  and  "  hot  odor,"  in  substantially  the 
same  manner  as  described  by  Drown  in  the 
Report  upon  the  Examination  of  Water  Sup 
plies  by  the  Mass.  State  Board  of  Health, 
1890,  Part  1. 

Color. 

The  dissolved  color  of  the  water  was  meas 
ured  by  the  platinum-cobalt  standards  of 
Hazen,  as  described  in  the  American  Chem 
ical  Journal,  Vol.  XIV,  page  300. 

O.v\gcn  Consumed. 

The  Kiibel  method  was  used  in  substan 
tially  the  same  form  as  described  by  Drown 
in  the  Report  of  the  Mass.  State  Board  of 
Health  for  1892,  page  328. 

In  this  determination  the  period  of  boiling 
with  potassium  permanganate  exerts  great  in 
fluence  on  the  results  obtained;  and.  further 
more,  this  period  differs  considerably  in  differ 
ent  laboratories.  It  was  the  custom  here  to 
boil  exactly  five  minutes  after  adding  the 
potassium  permanganate,  the  water  and  sul 
phuric  acid  having  been  previously  raised  to 
the  boiling  temperature.  In  order  that  the 
results  obtained  in  this  laboratory  may  be 
compared  with  previous  work  at  other  places, 


Oh 

Sample. 

III 
HCS 

•O  u 

io  Rh 

erw 

IO 

2 

5 
10 

2 

5 

10 

5-4 
6.8 
8-5 
1.9 
2-3 

2.8 

0.7 

1-4 
1-4 

filtered  without  coagulant 

with  coagulant.  .  • 



the  following  average  results  of  a  number  of 
experiments  are  presented. 

EXPERIMENTS  TO  SHOW  THE  EFFECT  OF 
DIFFERENT  PERIODS  OF  BOILING  ON  THE 
AMOUNT  OF  OXYGEN  CONSUMED. 


Nitrogen  as  Albuminoid  Ammonia. 

The  method  of  \Vanklyn  as  modified  by 
Drown,  Hazen,  and  Clark  was  used  substan 
tially  as  described  in  the  Report  of  the  Mass. 
State  Board  of  Health  for  1890,  Tart  II,  page 
710,  and  also  in  the  American  Chemical  Jour 
nal,  Vol.  XII,  page  425. 

Determinations  of  the  "  total  "  nitrogen  as 
albuminoid  ammonia  were  made  on  the  unfil- 
tered  water;  of  the  "  dissolved  "  after  the  pas 
sage  of  the  water  through  filter-paper  or  a 
Pasteur  filter.  And  the  "  suspended  "  nitro 
gen  as  albuminoid  ammonia  was  obtained  by 
difference. 

Nitrogen  as  Free  Ammonia. 

The  method  of  Wanklyn  was  used  as  de 
scribed  by  Drown.  Hazen,  and  Clark  in  con 
nection  with  the  nitrogen  as  albuminoid  am 
monia,  referred  to  above. 

Nitrogen  as  Nitrites. 

In  the  determination  of  nitrogen  as  nitrites 
the  Griess-Warrington  method  was  used,  as 
described  by  Drown  and  Hazen  in  the  Report 
of  the  Mass.  State  Board  of  Health  for  1890, 
Part  II,  page  715. 

Nitrogen  as  Nitrates. 

The  "  aluminum  method "  was  used  as 
modified  by  Hazen  and  Clark  and  described 


APPENDIX. 


447 


in  the  Report  of  the  Mass.  State  Board  of 
Health  for  1890,  Part  II,  page  711. 

The  following  method  was  employed  in 
the  preparation  of  nitrate-free  water  used  in 
blanks.  Eight  liters  of  ordinary  distilled 
water  were  treated  with  100  cubic  centimeters 
of  a  50  per  cent,  sodium  hydrate  solution, 
and  5  grams  of  pure  aluminum  foil.  After 
some  hours  the  water  was  placed  in  a  still  with 
3  grams  of  potassium  permanganate  and  dis 
tilled.  The  middle  portion  of  the  distillate 
was  free  from  nitrates. 

In  preparing  the  sodium  hydrate  solution 
one  liter  of  this  water  and  250  grams  of  the 
purest  sodium  hydrate  obtainable  were 
brought  together  in  a  porcelain  dish  with 
about  2  grams  of  pure  aluminum  foil.  When 
the  foil  was  all  dissolved,  the  solution  was 
boiled  down  to  a  volume  of  500  cubic  centi 
meters,  and,  after  being  allowed  to  settle,  fil 
tered  through  asbestos. 

Two  cubic  centimeters  of  this  solution  with 
50  cubic  centimeters  of  water  and  0.35  gram 
of  aluminum  foil,  should  indicate  the  pres 
ence  of  only  a  very  slight  amount  of  ammonia 
when  treated  in  the  same  manner  as  samples 
for  analysis. 

Chlorine. 

Chlorine  was  determined  according  to  the 
method  of  Mohr,  as  modified  by  Hazen  and 
described  in  the  American  Chemical  Journal, 
Vol.  XI,  page  409. 

Residue  on  Evaporation. 

For  this  determination  100  cubic  centi 
meters  of  the  water  were  evaporated  to  dry- 
ness  on  a  water  bath,  in  a  platinum  dish  of 
known  weight.  After  drying  in  a  steam  oven 
(temperature  96°  to  98°  C.)  for  two  hours, 
the  dish  with  its  contents  was  cooled  in  a 
desiccator  over  sulphuric  acid  and  weighed. 
This  gave  the  "total"  residue  on  evaporation. 
A  similar  determination  on  the  filtered  sample 
gave  the  "  dissolved  "  and  the  difference  be 
tween  these  two  gave  the  "  suspended  "  resi 
due  on  evaporation. 

Fixed  Residue  after  Ignition. 
The  fixed  residue  after  ignition  was  de 


termined  by  igniting  the  residue  on  evap 
oration  at  a  low  heat  in  a  radiator,  and 
weighing  as  usual  after  cooling  in  a  desicca 
tor. 

Alkalinity. 

The  method  of  Hehner  for  determining 
the  alkalinity  was  used  as  described  in  Leff- 
mann's  Examination  of  Water,  edition  of 
1895,  page  82.  Owing  to  the  fact  that  the 
color  of  the  Ohio  River  water  on  many  oc 
casions  obscures  the  end  point  when  methyl 
orange  is  used  as  an  indicator,  lacmoid  was 
employed  in  the  hot  sample.  Methyl  orange 
as  procured  at  this  laboratory  was  also  lacking 
in  sensitiveness.  Furthermore,  this  indicator 
is  incapable  of  showing  the  presence  of  unde- 
composed  sulphate  of  alumina,  a  property 
which  is  possessed  by  lacmoid. 

The  determinations  of  alkalinity  with 
lacmoid  as  an  indicator,  in  preference  to  tem 
porary  hardness  by  the  soap  method,  were 
necessary  in  this  work  for  two  reasons: 

1.  Normal    carbonates,    which    are    deter 
mined  as  permanent  hardness  or  incrusting 
constituents  by  the  soap  method,  have  the 
power  of  decomposing  sulphate  of  alumina  in 
the  same  manner  as  the  temporary-hardness 
constituents. 

2.  The  presence  of  undecomposed  chem 
icals  (sulphates)  in  the  effluent  is  not  shown 
by   the   ordinary    temporary-hardness   deter 
mination,  but  is  readily  detected  by  the  alka 
linity    determination    when    lacmoid    is    em 
ployed  as  an  indicator,  as  the  sulphate  of  alu 
mina  reacts  acid  to  this  indicator. 

The  alkalinity  determination,  therefore,  is 
a  measure  of  the  capacity  of  the  water  for  de 
composing  sulphate  of  alumina,  and  an  acid 
reaction  to  lacmoid  indicates  the  presence  of 
this  chemical  in  an  undecomposed  form. 

Incrusting  Constituents — Permanent  Hardness. 

The  salts  determined  by  the  Hehner  per 
manent-hardness  method  have  been  classed  as 
incrusting  constituents,  and  the  normal  car 
bonates  have  been  determined  as  alkalinity. 
The  reasons  for  this  are  presented  above. 
This  method  is  described  by  Leffmann  in 
Examination  of  Water,  edition  of  1895, 
page  82. 


448 


APPENDIX. 


Total  Hardness. 

In  regard  to  the  total  hardness  of  the  water 
as  indicated  by  its  soap-destroying  power,  the 
sum  of  the  determinations  of  the  alkalinity 
and  incrusting  constituents  is  comparable 
to  such  results,  although  not  necessarily  iden 
tical. 


For  the  determination  of  dissolved  alumina 
the  method  of  Richards  was  used  as  described 
in  Leffmann's  Examination  of  Water,  edi 
tion  of  1895,  page  58. 

Iron, 

For  the  determination  of  iron  the  general 
method  of  Thompson  was  used,  as  described 
in  Leffmann's  Examination  of  Water,  edi 
tion  of  1895,  page  57. 

Dissolved  Oxygen. 

The  method  for  the  determination  of  dis 
solved  oxygen  devised  by  Winkler  and  modi 
fied  by  Drown  and  Hazen  was  used  as  de 
scribed  in  the  Report  of  the  Mass.  State 
Board  of  Health  for  1890,  Part  II,  page  722. 

Carbonic  Acid  (Carbon  Dioxide). 

The  determination  of  carbonic  acid  (carbon 
dioxide)  in  the  water  was  made  according 
to  Trillich's  modification  of  Pettenkofer's 
method,  substantially  as  described  in  Ohl- 
miiller's  Untersuchung  des  Wassers,  edition 
of  1896. 

MINERAL  ANALYSES. 

Silica,    Barium,    Strontium,    Iron,    Aluminum, 
Nickel,  and  Manganese. 

The  methods  employed  in  the  determina 
tions  of  silica,  barium,  strontium,  iron,  alu 
minum,  nickel,  and  manganese,  were  as  fol 
lows: 

Silica. — One  or  two  liters  of  the  water  (de 
pending  upon  its  character)  were  acidulated 
by  the  addition  of  20  cubic  centimeters  of 


hydrochloric  acid,  and  evaporated  to  dryness. 
The  dish  containing  the  residue  was  trans 
ferred  to  an  air  bath,  and  .heated  to  130°  C., 
until  the  hydrochloric  acid  was  driven  off. 
There  were  then  added  10  cubic  centimeters 
of  hydrochloric  acid  and  150  cubic  centi 
meters  of  distilled  water,  and  the  whole  was 
gently  warmed.  The  silica  was  filtered  off, 
washed,  dried,  ignited,  and  weighed.  The 
residue  was  then  treated  with  hydrofluoric  and 
sulphuric  acids,  and  the  process  repeated. 
The  difference  in  weight  of  the  residue  before 
and  after  this  latter  treatment  was  taken  as 
the  amount  of  silica  present. 

Barium  and  Strontium. — Any  residue  re 
maining  after  the  treatment  with  hydrofluoric 
and  sulphuric  acids  was  fused  with  sodium 
carbonate,  and  the  barium  and  strontium  pre 
cipitated  and  weighed  together  as  sulphates. 

Iron  and  Aluminum. — The  filtrate  after  the 
removal  of  silica,  barium  and  strontium  was 
treated  for  iron,  manganese,  etc.,  as  follows: 
The  iron  and  aluminum  were  separated  by 
the  basic  acetate  method,  the  combined 
oxides  weighed,  and  the  aluminum  deter 
mined  by  difference,  the  iron  being  first 
determined  by  the  Thompson  colorometric 
method  already  referred  to. 

Nickel  and  Manganese. — The  filtrate  from 
the  iron  and  aluminum  determination  was 
rendered  slightly  acid  by  the  addition  of 
acetic  acid,  and  nickel,  if  present,  was  precipi 
tated  with  hydrogen  sulphide,  and  the  man 
ganese  separated  in  the  filtrate  after  neutral 
ization  by  the  addition  of  ammonium 
sulphide. 

Calcium  and  Magnesium. 

The  filtrate  from  the  manganese  determina 
tion  was  boiled  and  filtered  if  necessary,  and 
the  calcium  and  magnesium  determined  by 
precipitation  as  calcium  oxalate  and  mag 
nesium  pyrophosphate,  respectively. 

Sulphuric  Acid. 

One  liter  of  the  water  was  evaporated  to 
dryness  in  a  porcelain  dish  with  10  cubic 
centimeters  of  hydrochloric  acid.  The  silica 
was  removed  (see  silica  determination)  and 
the  sulphur  determined  by  precipitation  as 
barium  sulphate. 


A  I'l' END  IX. 


449 


The  phosphoric  acid  was  precipitated  from 
tlie  filtrate  obtained  in  the  determination  of 
the  sulphuric  acid  by  ammonium  molybdate. 
The  "  yellow  precipitate  "  \vas  dissolved  in 
ammonia  and  the  phosphorus  determined  as 
magnesium  pyrophosphate. 

Sodium  and  Potassium. 

Two  liters  of  the  water  were  evaporated  to 
dryness  in  a  platinum  dish  with  20  cubic 
centimeters  of  hydrochloric  acid.  The  residue 
was  taken  up  with  water,  a  few  crystals  of 
barium  hydrate  added  and  the  solution  boiled. 
The  solution  was  cooled  and  the  precipitate 
allowed  to  settle.  The  volume  was  then  made 
up  to  250  cubic  centimeters  and  200  cubic 
centimeters  were  filtered  off.  Ammonium 
carbonate  and  ammonium  oxalate  in  the 
solid  form  were  added  to  the  filtrate  and 
the  mixture  brought  to  a  boil.  After 
cooling  the  volume  was  again  made  up  to 
250  cubic  centimeters  and  200  cubic  centi 
meters  filtered  off.  Manganese  or  nickel,  if 
present  in  sufficient  amount  to  interfere,  were 
precipitated  as  sulphides. 

The  filtrate  was  evaporated  to  dryness  in 
a  platinum  dish,  sufficient  sulphuric  or  hydro 
chloric  acid  being  added  to  unite  with  the 
sodium  and  potassium.  After  ignition  to  ex 
pel  ammonium  salts,  redissolving  in  hot 
water,  filtering  and  evaporating  to  dryness, 
the  potassium  and  sodium  were  ignited  and 
weighed  as  sulphates  or  chlorides  according 
to  the  acid  added. 

The  percentages  of  potassium  and  sodium 
in  the  mixture  were  calculated  after  determin 
ing  the  common  constituent  (i.e.,  the  Cl  or 
SO:!)  from  the  formula  given  by  F.  K. 
Landis,  Jour.  Anier.  Chem.  Soc.,  Feb.,  1896. 

QUANTITATIVE  BACTKRIAI.  AXALVSKS. 

The  general  technique  of  the  quantitative 
bacterial  methods  used  in  these  investigations 
was  substantially  the  same  as  in  the  case  of 
those  described  by  Fuller  and  Copeland  in 
the  Report  of  the  Mass.  State  Hoard  of 
Health  for  1895,  page  585.  A  brief  summary 
of  some  of  the  principal  features  is  as  fol 
lows: 


At  the  outset  of  these  investigations  glycer 
ine  agar  was  used  as  the  culture  medium,  ow 
ing  to  its  adaptability  under  the  existing  local 
conditions.  The  laboratory  itself  had  a  widely 
variable  temperature,  owing  to  climatic  con 
ditions  and  to  the  presence  in  the  building  of 
a  number  of  steam-pipes  used  for  heating  and 
general  laboratory  purposes.  The  fact  that, 
at  a  number  of  points  on  the  steam-pipes  be 
tween  the  laboratory  and  the  boilers,  steam 
was  used  from  time  to  time  in  varying 
amounts  by  the  experimental  devices,  caused 
the  steam  pressure  to  vary;  and  in  conse 
quence  it  was  difficult  to  regulate  the  labora 
tory  temperature.  The  maintenance  of  a  uni 
form  temperature  in  the  thermostat  was 
difficult,  also,  on  account  of  the  necessity  of 
using  gasoline  gas  which  varied  widely  not 
only  in  quality  but  in  pressure. 

I'nder  these  circumstances  glycerine  agar 
was  at  first  selected  as  the  culture  medium 
with  the  view  to  getting  satisfactory  data 
upon  the  efficiency  of  the  filters  and  at  the 
same  time  preventing  heavy  losses  of  data 
which  seemed  imminent  with  the  use  of  gela 
tine.  The  precaution  was  taken,  however,  of 
making  comparative  studies  of  the  numbers 
of  bacteria  obtained  by  glycerine  agar  and 
gelatine,  respectively.  As  a  result  of  these 
studies  it  was  found  that  while  satisfactory 
data  could  be  obtained  for  comparing  the 
efficiency  of  the  several  filters,  yet  the  actual 
numbers  of  bacteria  were  normally,  but  not 
always,  materially  lower  when  glycerine  agar 
was  used  than  in  the  case  of  gelatine. 

Accordingly,  when  the  scope  of  the  investi 
gations  was  enlarged  on  Feb.  i,  1896.  it  was 
decided  to  adopt  nutrient  gelatine  as  the 
regular  culture  medium,  and  to  guard  against 
'loss  of  results  through  liquefaction  of  the 
medium  by  employing  a  sufficiently  low  tem 
perature  for  incubation. 

Reaction  of  Culture  Media. 

After  considerable  study  it  was  found  that 
the  reaction  of  media  used  in  the  regular 
quantitative  work  which  gave  the  most  satis 
factory  results  under  the  local  conditions  was 


45° 


APPENDIX. 


1.5  percent,  (equal  to  15  cubic  centimeters  of 
normal  hydrochloric  acid  added  to  every  liter 
of  neutral  medium),  especially  in  the  case  of 
the  effluent,  and  this  reaction  was,  therefore, 
maintained  throughout  the  tests.  The  rela 
tive  effects  of  reactions  ranging  from  0.5  to 
2.0  per  cent,  are  shown  in  the  following  table 
of  average  results: 

BACTERIA    PER   CUBIC   CENTIMETER    ON   GEL 
ATINE   OF    DIFFERENT   REACTIONS. 


Sampl 

liact 

ria  per  Cu 

)ic  Centim 

•ter. 

Number 
of 

Reaction  (r 

er  cents.t. 

0.5 

,.o 

i-5 

,.o 

Effluent  

41        > 

i    1 

IlS 

24S 

298 

243 

Sterilization. — All  glassware,  such  as  Petri 
dishes,  pipettes,  sample  bottles,  etc.,  were 
sterilized  for  one  and  one-half  hours  in  a  hot- 
air  sterilizer  at  a  temperature  of  150  degrees 
C,  or  a  little  higher.  All  media  and  water 
for  dilution  purposes  were  autoclaved  for  10 
minutes  under  a  steam  pressure  of  20  pounds. 

Dilution. —  In  the  case  of  the  river  water 
when  it  contained  high  numbers  of  bacteria, 
one  cubic  centimeter  of  the  sample  was  di 
luted  in  100  cubic  centimeters  of  sterile  dis 
tilled  water,  and  in  the  case  of  very  turbid 
effluents  a  dilution  of  i  to  10  was  used. 


The  normal  period  of  cultivation  em 
ployed  was  4  days  in  an  ice-chest  10  feet  long 
in  which  the  bacterial  compartment  and  ice 


compartment  were  in  the  opposite  ends.  In 
some  cases,  however,  when  the  temperature 
of  the  bacterial  compartment  fell  below  16  to 
18  degrees  C.,  a  longer  period  was  allowed 
in  order  that  the  maximum  growth  might  be 
more  nearly  obtained.  It  was  deemed  advisa 
ble  at  times,  owing  to  the  local  conditions 
facilitating  melting  and  liquefaction  of  the 
gelatine,  to  maintain  a  low  temperature 
in  this  compartment,  and  thus  guard  more 
effectively  against  the  possibility  of  loss  of 
plates  through  liquefaction.  Owing  to  this 
precautionary  procedure  the  loss  of  plates  due 
to  this  cause  was  trifling,  and  it  is  believed 
that  it  was  more  advantageous  to  prevent  the 
possibility  of  loss  of  data  upon  samples  which 
were  collected  under  conditions  which  might 
not  occur  again,  than  to  strive  at  all  times 
towards  the  maximum  possible  growth.  It 
is  to  be  noted,  further,  that  the  conditions 
were  the  same  for  all  samples  at  the  same 
time,  and  thus  strictly  comparable  results 
were  obtained  in  the  case  of  the  respective 
filters. 

The  relation  between  the  fourth  and  succes 
sive  day  growths  and  the  influence  exerted 
by  temperatures  ranging  from  10  to  18  de 
grees  C.,  are  indicated  by  the  results  and  per 
centages  presented  in  the  next  table.  In  1897 
temperatures  of  less  than  14  degrees  C.  were 
avoided  so  far  as  possible  by  partially  open 
ing  the  door  of  the  ice-chest  as  occasion  de 
manded.  So  far  as  our  knowledge  goes  the 
bacterial  results  obtained  during  the  investi 
gations  are  very  appreciably  higher  than 
would  be  obtained  by  two  days'  cultivation 
at  20  degrees  C.,  which  is  the  conventional 
procedure  in  Europe. 


SUMMARY   SHOWING  THE    RELATION    BETWEEN    FOURTH  ,   FIFTH-,  AND    SIXTH-DAY  GROWTHS 
OF    BACTERIA   ON    GELATINE    AT    DIFFERENT   TEMPERATURES. 


Number  of 

Range  of 

•*  per  Cublc  Ccn 

line    r. 

Samples 
Averaged. 

TD'ei>reere'sUc!" 

Source  of  Sample. 

Fourth  Day. 

Fiflll  Day. 

Sixth  Day. 

Fourth  to  FiflhDay. 

Fourth  to  Sixth  Day. 

27 

10-12 

River  water  
Effluent  

20  500 

29  600 
211 

31  700 
395 

44-4 
32.7 

54-6 
142.  i 

42 

12-14 

River  water  
Fffluent      .        ... 

23  ()OO 

32  700 

47000 

36.8 

96.7 

IO 

Fffluent 

33s 

7 
68 

16-18 

16-18 

River  water  
Effluent  

12  2OO 
155 

14  100 

167 

12  IOO 

170 

15.6 

7-7 

o.o 

9-7 

APPENDIX. 


45' 


In  the  next  table  are  presented  the  monthly  averages  of  temperatures  of  the  quantitative 
bacterial  compartment. 

MONTHLY     AVERAGES     OF    THE     TEMPERATURE     OF     THE     QUANTITATIVE    BACTERIAL 

COMPARTMENT. 


-895. 

1896. 

1897. 

Total 
Averages 

Nov. 

Dec.       Jan. 

Feb. 

Mar. 

Apr. 

May. 

June.  ;  July. 

Aug. 

Feb. 

Mar. 

Apr.      May. 

June. 

July. 

Maximum  .... 

22.0 

20.7      20.1 

12.8 

14.6 

14.2      16.9 

I6.S      19.4 

15." 

16.1 

15-2 

16.1 

>7-7 

19.5 

19.0 

17.3 

Minimum.  .  .    . 

19.6 

20.  2 

IQ.2 

10.7 

10.3 

II.7 

15.0 

I5.8 

16.7 

14.0 

I5.I 

14.0 

15-5 

15-5 

18.0 

16.7 

15.4 

Mean  

20.8 

20.4 

19.6 

II.  8 

12.5 

13.0 

16.0 

16.3 

18.0 

14.3 

15.6  I  14.6 

I5.S 

1  6.  6 

18.7 

17.9 

16.4 

Qualitative  Bacterial  Analyses. 

The  qualitative  bacterial  work  was  divided 
into  examinations  for  sewage  bacteria,  no 
tably  B.  coli  communis,  and  a  comparison  of 
the  species  of  bacteria  in  the  water  before  and 
after  purification,  with  an  incidental  classifica 
tion  of  the  more  common  forms  of  bacteria. 


For  this  purpose  the  methods  and  tests 
were  employed  as  found  in  the  best  manuals, 
and  they  were  usually  in  harmony  with  modi 
fications  suggested  at  the  Convention  of  Bac 
teriologists  held  at  New  York  in  June,  1895. 

Examinations  for  B.  coli  communis. 

The  method  of  procedure  in  the  search  for 
this  organism  was  substantially  the  same  as 
that  recommended  by  Smith  in  the  American 
Journal  of  the  Medical  Sciences  for  Sept., 
1895.  Dextrose  and  lactose  broths  were  both 
used  for  this  work  and  the  reactions  of  all  so 
lutions  used  in  the  fermentation  test  were  ad 
justed  to  an  alkalinity  of  1.5  per  cent.  A 
temperature  of  37  degrees  C.  was  employed 
in  all  the  tests  covering  the  examination  for 
this  species,  and  all  cultures  (with  the  excep 
tion  of  the  fermentation  cultures,  which  were 
allowed  to  develop  for  four  days)  were  al 
lowed  to  develop  for  48  hours  before  observa 


tions  were  made.  The  cultures  were  started 
in  flasks  containing  100  cubic  centimeters  of 
sterile  nutrient  dextrose  broth,  50  cubic  centi 
meters  of  water  being  used  each  time  for  in 
oculation.  Lactose  litmus  agar  plates  were 
made  from  these  cultures,  and  from  these 
plates  colonies  which  presented  in  two  days 
an  appearance  resembling  that  of  B.  coli  com 
munis  were  transferred  to  gelatine  tube,  agar 
tube,  peptone  solution,  litmus  milk,  and  fer 
mentation  tube.  Observations  were  made 
after  the  customary  period  of  two  days  on 
the  gelatine  and  agar  tube  cultures,  mi 
croscopically  for  si/.e  and  biologically  for 
a  characteristic  growth;  on  the  peptone 
solution  for  indol  production:  and  on  the 
litmus  milk  for  coagulation  both  before  and 
after  boiling.  The  fermentation  culture  was 
inspected  day  by  day,  the  quantity  of  gas 
recorded;  and  on  the  fourth  day  the  total  gas, 
the  percentage  of  carbon  dioxide,  and  the 
end  reaction  were  determined. 

COXVERSION  TABLES. 

There  are  given  in  the  next  tables  the  rela 
tions  which  exist  between  different  methods 
of  expression  of  several  quantities  which  are 
used  in  connection  with  this  report.  Conver 
sion  can  be  made  from  one  form  of  expression 
to  another  by  the  use  of  the  corresponding 
multiplication  factors  as  given  in  these  tables. 

Table  No.  II  is  copied  from  Kirkwood's 
Filtration  of  River  Water. 


452 


APPENDIX. 


TABLE  No.  I. 

CONVERSION    OF    STATEMENTS    OF    CHEMICAL    COMPOSITION. 


Grains  per  U.  S.  Gallon. 

Grains  per  British  Gallon. 
(277  cubic  inches.) 

Parts  per  ,00,000.             Parts  per  ,,000,000. 

i  grain  per  U.  S.  gallon  
i  grain  per  British  gallon  

I. 

0.830 
0.580 
0.056 

I.  2O 
I  . 

0.70 
0.07 

1.71                                     17.1 
1-43                               14-3 

I.                                                 IO.O 
0.  10                                                  I. 

TABLE  No.   II. 

EQUIVALENTS    OF    VARIOUS    MEASURES. 

Imperial 

Pounds 

Gallons. 

(Water  at  o°  C.) 

U    S   gallon 

o  8311 

8.3388822 

imperial   gallon  

I    .  20(J32 

I  . 

4-54346 

o.  16046 

0.004543 

277.274 

IO. 

08.31529 

,  . 

.... 

TABLE   No.    III. 

APPROXIMATE    EQUIVALENTS    OF    VARIOUS    MEASURES   OF    RATE    OF   FILTRATION. 


'       Vertical 

Million 

Million     !       Tr   c 

Velocity 

U.  S. 

British      i     rUj,S' 

British 

Cubic   Feet 

Vertical 

Vertical           •     -\j(,[..rs 

Gallons 

Gallons               iJi"5 

Gallons 

per 

Velocity 

Velocity     per  ;4  Hours 

per  Acre 

per  Acre     SquareFoot 

per 
Square  Foot 

SquarcYard 

in  Inches 

Millimeters  ^'ub'c  Meters 

24  Hours. 

24  Hours.      pl 

per  Hour. 

per  Hour. 

per  Hour. 

'per  Hour.'      ^^^7 

;     24  Hours. 

I  million    U.    S.   gallons    per    acre 

I  . 

0.833 

o.  06 

o.So 

1  .  15 

j  .  53 

39.0               0.935 

i  million  British   gallons   per  acre 

0  A  hours 

I  .  2OO 

I  .                        I  •  15 

O  .  96                    T  .  1  S 

1.84. 

46-  S 

I  .  122 

I  U.  S.  gdlon  per  square  foot   per 

I  .(>45 

o  .  S  70            T  . 

O.S3 

1  ,  2O 

i.  60 

40  .  7 

0.978 

i    British    gallon   per    square    foot 

1.255           i  •  (->45 

1  .  20 

1  .  44 

1.92 

48  .  9 

I  .  I~4 

i   cubic   foot  per  square   yard    per 

o.  724 

0.83 

o  .  69 

i  . 

i  .  33 

33  •  9 

0.813 

i  lineal  inch,  vertical  velocity,  per 

hour                       o.  652 

O-  543 

0.62 

o.  52 

o.  75 

i  . 

25.4 

o.  610 

i  hundred   lineal   millimeters,  ver- 

tic'il   vplori'v  ner  hour                              ^    ~f>fi 

o     T  TO 

9.16 

2  .  05 

2  .  95 

-\    OJ. 

IOO. 

2  .  400 

I    lineal    meter,    vertical    velocity 

-  •  »  j  ij             ---,.- 

J  •  VI 

per    24     hours  =  I    cubic    meter 

per  square  meter  per  24  hours.  . 

1  .  069 

0.891 

i  .02 

0.85 

1.23 

i.64 

41.7 

I. 

INDEX. 


Accessibility  of  pans 253,   443 

Agitation  of  surface  of  sand  layer 100,  274,  326,  443 

Agitator    75,8o 

Alg;e,   see    Microscopical      analyses,     uuJ     Biological 

character. 
Alkalinity,  determinations  of,  see  Chemical  analyses. 

increase  of,  by  permanganates 382 

reduction  of,  by  sulphates 42,  53,  384,   429 

Alum,  potash,   action  of,  as  a  coagulant 42,    380 

application  of,  by  Western  systems..    44,  47 
amounts  of,  see  Alumina,  sulphate  of. 

composition  of  lots  of,  used 41,    337 

cost  of,  comparative 380 

effect  of,  see  Alumina,  sulphate  of. 

preparation  of  solutions  of,   47,   251 

Alumina,  acetate  of,  action  of,   as  a  coagulant 380 

sulphate  of. 

effect  of  application  of 42,  53,  57 

on    cost    of  purifica 
tion  259 

on    quality    of    efflu 
ent,      42,      53-56, 

384,  427,   434 
amount     required     to     purify    Ohio    river 

water 270,  430,  441 

amounts  used  (ta8les) 269 

with  MacDougall  system. ...   323 
Jewell  system,   49,  196- 

204,   234,  240,  241 
Warren      system,       48, 

187-196,  232,  240,  241 
Water    Company's    de 
vices 342,  371-375 

Western      gravity    sys 
tem,  49,  204-207,  236, 

240,   241 

Western    pressure    sys 
tem,       49,      207-214, 

237,   240,   241 

composition  of  lots  of 40-42,   337 

cost     of,     annual     average    estimated,     to 

purify  Ohio  river  water 437 

comparative 437 

decomposition   of,  effects   of,   53,    244,  251, 

384,  428-434 
efficiency   of,    as   a   coagulant,    before  and 

,  after  decomposition 294 

efficiency  of,  comparative 413-419 

presence  of  undecomposed,  in  effluents..  55,  427 


Alumina,  sulphate  of, 

solutions  ot,  preparation  of.  .251,  259,  272,  440 
suitability    of,    as   a    coagulant   for    use    in 

purifying  Ohio  river  water 440 

see  also  Chemicals  and  Coagulants. 

Aluminate,  sodium,  action  of,  as  a  coagulant 380 

Aluminum,  cost  of,  as  metal  plates 299,  412 

sulphate '. 259,  299,   437 

see  also  the  various  compounds,  and  Elec- 
trolytical   preparation  of   aluminum  hy 
drate. 
Aluminum  hydrate,  efficiency  of,  as  a  coagulant,    when 

prepared  in  different  ways,  294,  413-416 
see  also  Electrolytical  preparation  of 

aluminum  hydrate. 

Ameiican  filters,  see  Filters,  American. 
Analyses,  see  specific  heading. 

Analytical  work,  methods  employed  in   445-451 

plan  of 10 

Anderson  process,  use  of,  with  Ohio  river  water 382 

Appurtenances    of    Warren,   Jewell,    Western     gravity 

and  Western  pressure  systems,  inventory  of 89-93 

Attention  given  to  the  respective  systems 107 

influence  of,  on  cost  of  treatment 267 

on  quality  of  the  effluent 258 

required    for   efficient    purification    of    Ohio 

river  water 271,    443 

Averages,  grand,  for  the  investigations  from  Oct.  1895, 

to  Aug.  1896 240 


B 


Bacteria,  effect  of  coagulants  on 

electricity  on 

in  city  tap  water  (table) 

in  effluent  of  (tables),  Harris  magneto-electric 

system 

Harris  Company's  devices.  282- 

Jewell    system,    148-169,    196- 

204,  234,  240, 

MacDougall     polarite    system, 
328, 

Warren    system,   128-148,   187- 
196,  232,  240, 

Water  Company's  devices,  350- 
366,   368- 

Western    gravity   system,    169- 

174,  204-207,  236,  240, 

Western  pressure  system,  174- 

186,  207-214,  238,  240, 

453 


179 

j  . 

841 

330 

a  M 

37 

241 

141 


454 


INDEX. 


Bacteria,  in  Ohio  river  water,  numbers  of  (table) 39 

species  of 37 

in  sand  layers ....    257 

passage  of,  through  filters 248 

Bacterial  analyses,  methods  of    449-451 

Biological  character  of  Ohio  river  water 16,  36-39 

after     purifica 
tion 248,   427 

Boilers,  u<e  of  purified  Ohio  river  water  in  ....  244,  429,  430 
Brownell,  see  Devices,  Marl;  and  Brownell. 


Carbon  dioxide,  see  Carbonic  acid. 

Carbonaceous     mailer,      amounts      of,      see     Chemical 

analyses. 

daily  removal  of,  by  Warren, 
Jewell,  Western  gravity, 
and  Western  pressure  sys 
tems  (tables) 223-227 

see  also  records  <•{  operation 
of   the    several   devices  and 
systems. 
Carbonate  of  lime,  effect  of  chemical  treatment  on,  see 

Alkalinity. 
Carbonic    acid,   amounts    of,  naturally   present   in   Ohio 

river  water 33,  34,  433 

cost  of  removal  of 434 

influence  of,  on  electrolytic  preparation 

of  iron  hydrate 391 

on  the  use  of  ferrous  com 
pounds  as  coagulants.  .   381 
in     purified   Ohio   river  water,    54,   244 

428,   433 
Caustic  soda,  see  Soda,  caustic. 

Chemical  analyses,  explanation  of 20,  32-35 

of    effluent    of,     regular     sanitary, 

(tables) 445-449 

Harris  system 279 

Harris  Company's  devices..  .282-289 

Jewell  system ...  117-122 

Mark  and  Brownell  devices,  310, 

3U,   316 

MacDougall  system 328 

Warren  system   1 12-1 17 

Water  Company's  devices 348 

Western  gravity  system 122 

Western  pressure  system.  .  .    124-126 
Ohio   river    water,    regular  sani 
tary 21-31 

special 32-35 

see  also  Carbonic  acid,  Incrusting 
constituents,  Mineral  analyses, 
and  Oxygen. 

Chemicals,  coagulating,  used,  see  Alum,  potash  ; 
Alumina,  sulphate  of; 
Iron,  persulphate  and 
protosulphate  of;  and 
Electrolytic  prepara 
tion  of  coagulants. 
see  also  Coagulants. 


Chemicals,  commercial,  available  as  coagulants.  ...378,   385 

Chloride  of  alumina,  use  of,  as  a  coagulant 380 

Chlorine,  application  of,  with  Jewell  system 46 

Clay  exiraclor,  see  System,  MacDougall  polarite. 
Cleaning,  set  part  in  question. 

Clearness,  degree  of,  explanation  of 215 

of  effluent  of  (tables), 

Jewell   system,    117- 

122,  196-204 

MacDougall  system.   329 
Mark  and    Brownell 

devices.  .310,   314,   316 
Warren  system,  1 12- 

117,   222 
Water       Company's 

devices..  .348,  371-375 
Western  gravity  sys 
tem  122,   222 

Western         pressure 
system...  124-126,    222 

Coagulants,  absorption  of,  by  silt  and  clay m 383 

action  of  various 381 ,   384 

effect  of,  on  cost  of  purification 258 

on  quality  of  purified   water,  42, 

53-56,  384,  405,  429,   431 

application   of 324 

devices  for,  42-46,  260,  272, 

338-341 

uniformity  of 251,   260 

amount  required,  effect  of  character  of  sus 
pended  matter  on 384 

to     purify      Ohio      river 

water 273,  422,  430,   441 

cost  of  available,  annual  average  to  purify 

Ohio  River  water.    .  .  .   437 

comparative 435 

economical  application  of,  to  aid   in  sedi 
mentation  416 

efficiency  of  available,  comparative. . .    382,  413 
relative,     of      those 
absorbed  and  not 
absorbed  by  clay..   384 
different   amounts   of,  in   sedi 
mentation  418 

germicidul  action  of 383 

kinds  of,  used 40-42,  259,  310,  323,  337 

loss  of,  when  applied  in  small  quantities...   384 
maximum  safe  amount  of  (with  Ohio  river 
water)  electro- 
lytically      pre 
pared   hydrate 

of  iron 397 

sulphates 383 

metals  available  as 378 

most  suitable  one  for  use  in  the  purification 

of  Ohio  river  water 440 

necessity  of  use   of,   to   purify  Ohio   river 

water 40,  439 

point  of  application  of 441 

reaction  of,  speed  of 383 

waste  of 384 


INDEX. 


455 


Coagulation,  application  of,  to  Ohio  river  water 57 

degree  of 253,  262,  422,  440 

devices  for 58-61,  qi,  272,  336 

effect  of   252,  261,  273 

period  of   273,  440 

effect  of 262,  419 

process  of 57 

see  also  Filtration  and  Sedimentation. 

Conditions  of  these  tests 1 1 

Contents,  table  of iii-vii 

Controller,  automatic,  of  Jewell  system 79 

Copperas,  see  Iron,  protostilphnte  of. 

Corrosion  of  iron  by  purified  Ohio  river  water 244.  428 

partial     protective    influence    of    sus 
pended  matter  against 428 

lead  by  Ohio  river  water 434 

D 

Decomposition  of  aluminum,  electrolytic,  see  Electro 
lytic  preparation  of  alu 
minum  hydrate. 

chemicals,  sec  the  specific  compound, 
iron,     electrolytic,     see     Electrolytic 

preparation  of  iron  hydrate. 
Delays,   table  of,  of  Warren,  Jewell,   Western  gravity 

and  Western  pressure  systems 94 

Deposition    of    metals,    in    electrolysis,    see   Electrolytic 

preparation  of  aluminum  and  iron  hydrates. 
Devices  arranged  by  the  Water  Company  in  1897, 

adaptation    of    construction    to    existing    con 
ditions 341 

analyses  in  connection  with,  bacterial 350-366 

chemical 348 

see  also  Water, 
Ohio  river,  an 
alyses  of. 

chemicals,  kinds  of,  used 337 

coagulants,  quantity  of,  used 259,  342 

comparison  of  coagulants 342 

conditions  and  methods  of  operation 341-346 

description,  general,  of 335 

discussion  of  results,  plan  of 375 

electric  generating  appliances 338 

electrodes 339 

electrolytic  cells. 338 

filter 341 

filtration,  rate  of 342 

interruptions  of  tests   341 

objects  of  tests 334 

operation,  summary  of  results  of  (table)...   371-374 

periods  of  operation 342 

plans  for  testing 292 

results  accomplished,  general  description  of..  .   346 

results,  plan  of  presentation  of 334 

runs,  length  of 342 

special  notes  on   345 

sedimentation,  devices  for 335 

removal    of    bacteria   and    sus 
pended  matter  by 37°-3?8 

Devices,  mechanical,  to  aid  in  the  operation  of  the 
Warren,  Jewell,  Western  gravity  and  Western  pres 
sure  systems. ... .  ...  105-107 


Devices  of  Harris  Company  : 

Device  No.  I,  bacterial  analyses  in  connection  with.   282 
chemical  analyses  in  connection  with    282 

description  of 281 

electric  appliances 281 

electrodes 281 

magnets,   electro- 281 

operation  of 282 

stand  pipe 281 

Device   No.  2,  description  of 282 

results  accomplished 283 

Device  No.   3,  description  of 283 

filter 284 

operation  of 284 

results  accomplished 284 

Device   No.   4,  aluminum  used  with 286 

description  of 285 

operation  of 286 

results  accomplished 286 

Device  No.   5,  aluminum  used  with 290 

bacterial  analyses  in  connection  with.   288 
chemical  analyses  in  connection  with  28q 

description  of 287 

operation  of 287 

results  accomplished 289 

glass  jar  experiments 280 

Devices  of  Mark  and  Brownell  : 

bacterial  analyses  in  connection  with    ..   308,  314 
Brownell  electrodes,  results  accomplished  with  309 

Brownell  cell,  description  of 304 

passage    of     untreated     water 

through 306 

chemical  analyses  in  connectionwith...  309,  314, 316 
comparison  of  efficiency  of  filtration  of  water 
treated  by  Brownell  electrodes,    with   that 

of — water  without  treatment 313 

water    treated    by   similar    aluminum 

electrodts 315 

conclusion  in  regard  to 313 

construction  of 304 

electrical  connections 305 

electric  generating  appliances 304 

electrodes 305 

electrolytic  cells 304 

loss  of  hydrate  by  construction  of  cells 311 

Mark  electrodes,  operation  of 306 

metal  decom posed   310 

plans  for  investigation  of 303 

preliminary  experiments  leading  to 301 

unofficial  runs  of 307 

Devices,  Palmer  and   Brownell,  see  Devices,  Maik  and 
Brownell. 


Electric  aluminum   process,  see  Electrolytic  preparation 

of  aluminum  hydrate. 

Electric  generating  appliances,  cost  of  construction  of..     435 
operation  of. . . .     436 
jet  also   Devices  of  Mark 
and     Brownell,   and 
System,   Harris. 


456 


INDEX. 


Electric  iron  process,  see  Electrolytic  preparation  of  iron 

hydrate. 

Electric   power   required    for    the    purification    of  Ohio 

river   water  by  the    use  of 

electrolytically    prepared 

iron  hydrate 436 

the  preparation    of    alumi 
num    hydrate  electrolyti- 

cally  (1896  data). 302 

used  in  the  Mark  and  Brownell  devices.   312 
Water  Company's  devices. .   370 
waste  of,  in  the  electrolytical  prepara 
tion  of  coagulants 404.  4Og 

Electric  resistance,  of  coat  ings  on  plates,  of  aluminum.  411,412 

iron 404 

Ohio  river  water 312,  390 

solutions  of  various  salts 393 

Electricity,  effect  of,  on  bacteria  and  organic  matter.  . .    292 

in  purifying  Ohio  river  water 293 

Electrodes,  active 389 

iron,  cost  of  construction  of 436,  603 

passivity  of    391 

polarization  of 391 

see  also  Devices,  Harris  Company,  Mark  and 
Brownell,  Water  Company;  and  Sys 
tem,  Harris. 

Electrolysis,  general  description   of 388 

Electrolytic  cells,  cost  of  construction  of- 435 

see  also  same  as  for  electrodes. 
Electrolytic  decomposition,  see  Electrolytic  preparation 

of  coagulants. 
Electrolytic  preparation  of  aluminum  hydrate, 

conclusions  in  regard  to,  lSy6 308 

1897 412 

cost  of  the  hydrate  as  compared  with  that 
prepared  by  the  decomposition  of  the 

sulphate  (1896  data)   291) 

decomposition  of  the  positive  plates..  296,406 
deposition  on  the  negative  plates.  .  . .  299,  408 

description  of 406 

direction  of  the  electric  current,  influence 

of  reversing  the 410 

efficiency  of  the  coagulant 413-416 

formation  of  gas 402 

influence   of  the  composition  of  the   river 

water 406 

magnets,  electro-,  effect  of 296 

metal  wasted 299,  411 

passivity  of  electrodes (06 

power  wasted 412 

regularity  of  formation  of  hydrate 299 

scale,  influence  of  the  composition  of  the 

river  water  on  the  formation  of.   410 

presence  of 410 

Electrolytic  preparation  of  coagulants, 

advantages  of 300,  313,  387 

electric  laws  of 390 

polarization  of  electrodes 391 

relative    efficiency  of   iron    and    aluminum 

electrodes  in 315 

secondary  reactions 392 

see  also  Electrolysis. 


Electrolytic  preparation  of  iron  hydrate, 

effect   of    ill  •    process    on    subsidence   and 

filtration 405 

amount    of    treatment    required    to     purify 

Ohio  river  water 430 

carbonic  acid,  influence  of 395 

conclusions  in  regard  to,  at  the  close  of  the 
i  n  vestigations 
of  the  Mark  and 
Brownell  de 
vices 313 

at     the     close    of 
the     entire     in 
vestigations  . .  .    405 
cost    of,    annual    average,    to    purify   Ohio 

river  water 436 

cost  of,  comparative 436 

current  density,  influence  of 402 

decomposition  of  the  positive  plates.  .   310,    396 

deposition  on  the  negative  plnles 398 

effect  of  allowing  the  electrodes  to  remain 

out  of   service     ...   404 

efficiency  of  the  coagulant    413-416 

electric    current,   direction    of,    influence  ou 

reversing  the 403 

electric  resistance  of  films  of  oxide 404 

form  in  which  the  iron  leaves  the  cell 396 

plales. .  .    395 
hydrate,  rate  and  uniformity  of    formation 

of  available 398 

hydrogen,  influence   of 396 

limitations  of 397 

metal  wasted 396,  404 

oxygen,  influence  of 395 

passivity  of  electrodes    31)3 

potential,  influence  of   399 

power  wasted 404 

river  water,  influence  of  the  composition  of  403 
solubility  of   initial    iron   compounds,  influ 
ence  of 396 

see  also  Devices  of   Mark  and  Brownell,  and 
of     Water    Company,    and      Electrolytic 
preparation  of  coagulants. 
English  fillers,  see  Filters,  English. 
European  filters,  s,-c  Filters,  European. 


Filter,  set  the  various  systems  and  devices. 
Filtered  water  exits,  see  Strainer  system. 

Filters,  American  type,  efficiency  and  cost  of 10-1 1 

general  description  of 10,  70 

relative    adaptability     of,     for 
purification     of    Ohio    river 

water (39 

types  tested 70 

English  type  of 5-9 

relative  adaptability  of,  for  puri 
fication  of  Ohio  river  water. .   439 

Filtration,  effect  of  period  of  coagulation  on 419-421 

use   of  electrolytically  prepared   co 
agulants  on 404 


INDEX. 


457 


Filtration,  conditions  for  successful,  by  American  filters, 

422-426 

degree  of  coagulation  for 422 

minimum  amount  of  coagulant  required  for, 
of  Ohio  river  water  by  American  filters.  . .    430 

principals  of  sand,  without  coagulants 7 

rate  of 254.264,   274 

required      for      purification     of     Ohio     river 

"'•'ter    441 

special  devices  for  regulating  the  rate  of. ...    iu6 
Freshets  in  the  Ohio  river,  effect  of,  on  the  composition 

of  the  water 15 

records  of  (table)      16-17 


Gases,  in  purified  Ohio  river  wate 
Germicidal  action  of  coagulants.  . 


Listing    constituents, 


its    of,    in    Oh 


water 33-35 

water  supplies  of 
various  cities...   433 

cost  of   removal  of 434 

increase   of,   due    to   the   use    of 

sulphates  as  coagulants.  .    54,  432 
in  purified  Ohio  river  water.  ..54,  432 

Investigations,  outline  of  entire 1-2 

Ions,  see  F.lectrolysis. 

Iron,  application  of.  with  Jewell  system 46 

compounds,    influence     of    the     solubility    of    the 
unoxidizcd,  on  the  electrolytic  prepara 
tion  of  iron  hydrate 30,6 

on  their  use  as  coagulants 381 

metallic,    by   the   Anderson    process,   applicability 
of,  in    the    pnrilication    of    Ohio 

river  water.  .  .      382 

persulphate  of,  action  of,  as  a  coagulant 381 

composition  of  lot  of,  used  by  the 

Water  Company  in  1897 337 

cost  of,  annual  average  estimated, 
for  the  purification  of  Ohio  river 

water 437 

effect   of,    on    the    quality   of    the 


Jewell  system,  see  System,  Jewell. 


MacDougall  system,  see  System,  MacDougall  polarite. 
Magnets,  Electro-,  effect  of,  on  the  rate  of  electrolytic 
formation      of     aluminum 

hydrate 296 

s,'e  also  Devices,  Harris  Company  ; 
and    System,    Harris    mag 
neto-electric. 
Manganese,  permanganates  of  lime  and  potash, 

action  of,  as  coagulants 382 

cost  of 382 

effect  of 382 

Microscopical  analyses  of  effluents  (tables) 127 

Ohio  river  water  (table)  ..    36-37 


Ohio  river  water,  see  Water,  Ohio  river. 

Operation,    manner    of,    of    Warren,    Jewell,    Western 

gravity  and  Western  pressure  systems...  96-105 
records   of,    .«•<•   the    several    systems    and 

devices. 
Organic  matter,  amounts  of,  see  Chemical  analyses. 

effect  of  electricity  on 292 

removal  of,  by  Warren,  Jewell,  Western 
gravity       and      Western      pressure 

systems  . .    223-227 

Oxygen  consumed,  see  Carbonaceous  matter. 

influence  of,  on  the  electrolytic  preparation  of 

iron  hydrate 392 

in  Ohio  river  water 33 

after  purification  by 
Warren,  Jewell,  Western 
gravity  and  Western 

pressure  systems 243 

influence  of  the  use  of 
electrolytically  prepared 
coagulants  on  the 
amount  of,  after  purifica- 
t'°» 43" 


purified  water 381,432 

efficiency  of,  as  a  coagulant. .   413-416  Passivity,  see  Electrodes,  passivity  of. 

protosulphate  of,  action  of,  as  a  coagulant   381  i    Periods,   outline   of   the   twenty,    into    which    the   in- 

composition    of   lot   of,   used    by  vestigations    from    Oct.    1895     to    Aug.    1896    were 

the  Water  Company,  in   1897.   337  divided 216-219 


INDEX. 


Permanganates,  see  Manganese. 

Persulphate  of  iron,  see  Iron,  persulphate  of. 

Polarite,  see  System,  MacDougall  polarite. 

Potash  alum,  see  Alum,  potash. 

Pressure,  see  Head. 

Prodigiosus,    B.,   passage   of,   through   Warren,  Jewell, 

Western  gravity  and  Western  pressure  filters 2.49-250 

Protosulphate  of  iron,  see  Iron,  prolosulphale  of. 

Purification  of  water,  outline  of  history  of 5 

see  also  Coagulation,  Filtration, 
Sedimentation,  and  the  several 
systems  and  devices. 


R 

Rate  of  filtration,  see  Filtration,  rate  of. 
Regulators,  see  the  several  systems  and  devices 
Repairs,  see  the  several  systems  and  devices. 
Resistance,  electric,  see  Electric  resistance. 
Ruhmkorff  coil,  see  System,  Harris  magneto-electric. 

S 

Samples,  manner  of  collection  of 18,  445 

Sand  layer,  area  of  surface  of,  of  Jewell  filter 79 

Warren  filter 74 

Western    gravity    fil 
ter 83,  84 

Western  pressure   fil 
ter  87 

character  of,  for  successful  filtration  of  Ohio 

river  water  by  American  filters 426,  442 

cleaning,  devices  for 274,  443 

Jewell  system 79 

Warren  system 74 

Western   gravity  sys- 


tei 


Western  pressure  sys 
tem  88 

influence   of.    on  cost  of   purifica 
tion 264 

quality  of  effluent  256 
manner  of  operation   of,   98,  101, 

103,  104,  321,  323,  343 

water  used,  kind  of 256 

kind  of  sand  used,  influence  of 253,  262 

Jewell  filter 79 

Warren   filter 73 

Western    gravity    filter, 

82.  84 
Western    pressure    filter    87 

location  of 273,    371 

thickness  of,  influence  of 253,  262 

Jewell    filter 79 

Warren  filter 73 

Western  gravity  filter 82,  84 

Western  pressure  filter 87 

Sedimentation,  necessity  of,  with  Ohio   river  water.  .  .      383 
plain,  bacteria  in  city  lap  water  (table).     69 
purification  of  Ohio    river  water 
by 252,  261,  440 


-Sedimentation, with  coagulation,  effect  of  use  of  electro- 
lytically       prepared 
hydrate  of  iron  on. .    414 
coagulants   to  aid   416-419 
provisions  for,     57-64, 

9',  335 
influence 
of,  252,    261 

process  of 57 

purification      of      Ohio 
river    water    by,  58, 

65-69,  78,  271,  367,  440 

Soap,  amount  required  with  purified  Ohio  river  water..   432 
Soda,  CHUstic,  composition  of  lot  of,  used  by  the  Water 

Company  in  1897 338 

to  clean  sand  layer 426,  443 

remove  incrusting  constituents 433 

Spark  drum,  see  System,  Harris  magneto-electric. 

Storage  of  purified  Ohio  river  water 427,  443 

Strainer  system  of 4-I2 

Jewell  filter. 78 

Warren  filter 72 

Western  gravity  filter 82,  83 

Western  pressure  filter 86 

Sulphate  of  alumina,  see  Alumina,  sulphate  of. 
Sulphates   of    lime   and   magnesia,   see  Incrusting  con 
stituents. 
Summaries,  of  results  of  investigations  from  Oct.  1895 

to  Aug.  1896,  explanations  of 215-221 

tables  of 222-241 

Suspended  matter  in  water  for  successful  filtration 422 

partial    protective    influence 
of,    against   corrosion    of 

iron 428 

see  also  Chemical  analyses. 
System,  Harris  magneto-electric, 

bacterial  analyses  in  connection  with 279 

chemical  analyses  in  connection  with 279 

description  of,  general 276 

electric  circuits 278 

electric  generating  appliances 278 

efficiency  of. . .  .   290 

electrodes 277 

electrolytic  cells 276 

magnets,  electro   277 

operation  of 278 

spark  drum 276 

status  of,  July  I,  1896 281 

System,  Jewell, 

alumina,  sulphate  of, 

amounts  of  (table),  by  days 50 

by  runs  196-204 

composition  of  lots  of 41 

devices  for  application  of. ...   42-46 
solutions  of,  strength  of  (table)     47 

appurtenances  of,  inventory  of 9°-93 

attention  given  to    107 

chlorine,  application  of   t  .  . .     40 

efficiency  of,  bacterial,  average  by  days...  .228-231 

runs. .  ..196-204 

removal  of  organic  matter 223-227 


INDEX. 


459 


System,  Jewell— ConcluJeii. 

effluent  of,  analyses  of,  bacterial 148-169 

chemical 117-122 

microscopical 127 

mineral 127 

bacteria  in,  see  bacterial  efficiency, 
clearness  of,  average  daily  degree 

of ....     222 

filter  of,  agitator So 

controller,  automatic 79 

description  of,  general .      77 

filter  tank 77 

prodigiosus  B.,  application  of,  tn. .  .  .   249 

sand  layer,  area  of  surface  of 79 

bacteria  in 257 

device  for  cleaning 79 

kinds  of  sand 79 

nitrogen    as    albuminoid 

ammonia  in 257 

thickness  of 79 

strainer  system 78 

iron,  application  of  metallic 46 

lime,  amounts  used,  average  by  clays 52 

devices  for  the  application  of 45 

solutions  of,  strengths  of 52 

operation  of,  delays  of 94 

manner  of 99 

records  of,  description  of  tables.,   no 
summaries     of,     234, 

240,   241 

tables  of 196-204 

regulating  devices,  special 105 

repairs  of 93 

sedimentation  with  coagulation,  devices  for.. . .      59 
purification  by     61 

time  occupied  by 95 

System,  MacDougall  polarite, 

alumina,  sulphate  of,  application  of.  . 
bacterial  analyses  in  connection  with. . 
bacterial  results,  summary  of,  by  days, 
chemical  analyses  in  connection  with. . 

see  also  Water,  Ohio  river. 

chemical  results,  summary  of,  by  days 328 

clay  extractor 319 

conclusions  in  regard  to 327 

description  of,  general 318 

efficiency  of,  summary  of,  by  days 328 

effluent,  quality  of 323 

iron  tank  with  baffle  plates   318 

operation  of 32 1-326 

polarite,  analysis  of 322 

polarite  filter,  description  of 320 

effect  of  air  pocketing  in. .  . 

filtering  materials  of 

modifications  of 

System,  Warren, 

alumina,  sulphate  of, 

amounts  of  (tables),  by  day: 

by  runs..  187-196 

composition  of  lots  of 41 

devices  for  the  application  of. ...     42 
solutions  of,  strength  of  (tables).     48 


321 
322 
321 


" 


System,  Warren-  Concluded. 

appurtenances  of,  inventory  of 9'^~93 

attention  given  to 107 

efficiency  of,  bacterial,  average  by  days  . .    228-231 

runs.    .    187-196 

removal  of  organic  matter.  .    223-227 

effluent  of,   analyses  of,  bacterial 128-148 

chemical 112-1 17 

microscopical 127 

mineral 127 

bacteria  in,  see  bacterial  efficiency, 
clearness    of,     average   daily   de 
gree  of 22: 

filter  of,  agitator 75 

description  of,  general 71 

filter  tank. 71 

filtered  water  chamber 73 

prodigiosus  R.,  application  of.  to  ....    249 

sand  layer,  area  of  surface  of 74 

bacteria  in 257 

device  for  cleaning 74 

kinds  of  sand 73 

nitrogen      as    albuminoid 

ammonia  in 257 

thickness  of 73 

strainer  system 72 

weir 73 

operation  of,  delays  of 94 

manner  of 96 

records  of,  description  of  tables   no 
summaries  of,      232, 

240,  241 

tables  of 187-196 

regulating  devices,  special 105 

repairs  of 93 

sedimentation  with  coagulation,  devices  for...      58 
purification  by     61 

time  occupied  by 95 

System,  Western  (parts  common  to  both), 

appurtenances,  inventory  of 90-93 

attention  given  to 107 

chemicals  used 41 

amounts  of  potash  alum  used. .      51 
sulphate  of  alumina 

used  (table) 51 

solutions  of,  strength  of  (table)     49 
sedimentation  with  coagulation,  devices  for. ,  .     60 
purification  by     63 
System,  Western  gravity, 

appurtenances  of,  inventory  of 90-93 

chemicals   used,  average  amounts  of,    by  runs, 

204-207 

efficiency  of,  bacterial,  average  by  days..   228-231 

average  by  runs. . .  204-207 

removal  of  organic  matter...   223-227 

effluent  of,  analyses  of,  bacterial      '"9-174 

chemical 122 

microscopical 127 

mineral 127 

effluent  of,  bacteria  in,  sre  bacterial  efficiency, 
clearness  of,  average  daily  degree 

of...  .  .     222 


INDEX. 


System,  Western  gravity — Concluded. 

filter  of,  description  of  filters  (A)  and  (H) Si 

prodigiosus  B.,  application  of,  to  ....   249 

filter  (A),  description  of 82 

filter  tank  .  , 82 

sand  layer,  area  of  surface  of 83 

bacteria  in 257 

device  for  cleaning 83 

kinds  of  sand 83 

nitrogen     as    albuminoid 

ammonia  in 257 

thickness  of 82 

strainer  system 82 

filter  (B),  description  of 83 

filter  tank 83 

sand  layer,  area  of  surface  of 84 

bacteria  in 257 

device  for  cleaning 84 

kinds  of  sand 84 

nitrogen     as     albuminoid 

ammonia  in 257 

thickness  of 84 

strainer  system 84 

operation  of,  delays  of 94 

manner  of 102,    103 

records  of,  description  of  tables.,    no 
summaries     of,     236, 

240,   241 

tables  of   204-207 

regulating  devices,  special 105 

repairs  of 93 

time  occupied  by 95 

see   also   System,  Western   (parts   common    to 

both). 
System,  Western  pressure, 

appurtenances,  inventory  of 9°~93 

chemicals  used,  average  amounts   of,  by  runs, 

207-214 

efficiency  of,  bacterial,  average  by  days..  .   228-231 

runs...   207-214 

removal  of  organic  matter .  .   223-227 

effluent  of,  analyses  of,  bacterial 174-186 

chemical 124-126 

microscopical 127 

mineral 127 

bacteria  in,  see  bacterial  efficiency, 
clearness   of,  average  daily  degree 

of. 222 

filter  of,  description  of,  general   85 

filter  chamber 86 

prodigiosus  B.,  application  of,  to,.    .   249 

sand  layer,  area  of  surface  of 87 

bacteria  in 257 

device  for  cleaning 88 

kinds  of  sand 87 

nitrogen     as     albuminoid 

ammonia  in 257 

thickness  of 87 

strainer  system 86 

operation  of,  delays  of 94 

manner  of 104 

records  of,  description  of  tables,    no 


System,  Western  pressure — Concluded. 

operation  of,  records  of,  summaries  of,  238,240,241 

tables  of 207-214 

regulating  devices,  special 105 

repairs  of 93 

time  occupied  by    95 

Systems  of  purification  investigated 1-4 


Tables,  see  specific  topic. 

Tap  water,  city,  bacteria  in  (table) 69 

Tests,  from  Oct.  1895  to  Aug.  1896,  conditions  of n 

outline  of I 

Time  occupied  in  various  ways  by  the  Warren,  Jewell, 

Western  gravity  and  Western  pressure  systems... .   93-95 
Totals,  grand,  for  the  investigations  from  Oct.  1895  to 

Aug.  1896 240 


U 


Warren  system,  see  System,  Warren. 
Water,  Ohio  river,  after  purification, 

appearance  of 242,  426 

adaptability  for  boiler  use,  245,  429,432 

biological  character  of 248,  427 

carbonic  acid  in  ....    53,  244,  431-434 

color  of 243 

corrosion  of  iron  by 244,  43I~434 

lead  by 434 

mineral  matter  in 426 

odor  of 243,  426 

organic  matter  in 243,  426 

oxygen,  dissolved,  in 243,  427 

soap  required 432 

storage  of 427,  443 

taste  of 243,  426 

undecomposed  coagulants  in 427 

uniformity  of  quality  of 429 

analyses  of,  bacterial 39 

chemical 21-31 

microscopical 36 

mineral 34 

application  of  coagulation  to 57 

character  of,  general 15 

biological,  16,  36-39 
chemical,  16,  20-34 
factors    affect 
ing  the 15 

physical 1 8 

composition  of,  bacteria  in,  numbers 
of,  see 
bacterial 
analyses, 
species  of  36 
carbonaceous  matter 

223-227 

influence  of,  on  the 
electrolytic  prep 
aration  of  coag 
ulants 403,  410 


IhDEX. 


461 


Water,  Ohio  river,  afier  purification — Concluded. 

composition  of,  nitrogen      as    albu 
minoid  ammonia 223-227 

factors  which  influenced  the  quality 
of,     after     purification,     250-257, 

405,  43'-434 
purification  of,  accessibility  of  parts 

of  system    443 

applicability  of  meth 
ods     investigated, 

271,  439 

attention     required,    258, 
2(^7,  443 
coagulant,      amount, 

273,  430,  441 

kind 440 

imperative 
ness      of 
use  of. .    439 
point  of  ap 
plication 


Water,  Ohio  river,  purification  of,  cost  of,  coagulant  for, 

4S5--437 

elements  of.. .    268 
factors   which 
affected  the.   267 

filters  for 442 

filtration 422-425.441 

sand  layer  for. .  .426,  442 
cleaning 

of. .424,  443 
location 

of 442 

sedimentation,  plain, 
359.  37<> 

-378,   44° 
with     co 
agula 
tion  ...   440 
Weir  used  in  ihe  Warren  system 73 


;.,       A         I        II 


II         I        II 


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'SECTION     OF    JEWELL    GRAVITY     SYSTEM." 


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